Hydrogenation of oxygenated molecules from biomass refining

ABSTRACT

The present disclosure relates to methods, processes, and systems for utilizing the dehydrogenation of 2-butanol for hydrogen consuming reactions of biomass or biomass-derived molecules. The present invention relates to methods, processes, and systems for utilizing the dehydrogenation of 2-butanol for hydrogen consuming hydrogenation, hydrogenolysis, or hydrodeoxygenation reactions of biomass or biomass-derived molecules.

CROSS-REFERENCE

This application claims the benefit of U.S. Provisional Application No.61/992,131, filed May 12, 2014, which is incorporated herein byreference in its entirety.

INCORPORATION BY REFERENCE

All publications, patents, and patent applications mentioned in thisspecification are herein incorporated by reference to the same extent asif each individual publication, patent, or patent application wasspecifically and individually indicated to be incorporated by reference.

FIELD OF THE INVENTION

The invention relates to the hydrogenation, hydrogenolysis, andhydrodeoxygenation of biomass derived molecules.

BACKGROUND OF THE INVENTION

Industrial chemicals obtained from inexpensive sources are desirable foruse in industrial processes, for example, as raw materials, solvents, orstarting materials. It has become increasingly desirable to obtainindustrial chemicals, or their precursors, from materials that are notonly inexpensive but that are also more environmentally friendly. Ofparticular interest are materials that can be obtained from renewablesources, such as materials that are produced by a biological activitysuch as planting, farming, or harvesting.

SUMMARY OF THE INVENTION

The present invention relates to methods, processes, and systems forutilizing the dehydrogenation of 2-butanol for hydrogen consuminghydrogenation, hydrogenolysis, or hydrodeoxygenation reactions ofbiomass or biomass-derived molecules.

Provided herein are methods for using 2-butanol as the hydrogen sourcefor a conversion reaction. The methods can comprise: dehydrogenating2-butanol to yield 2-butanone; wherein hydrogen removed from the2-butanol during dehydrogenating is the hydrogen source for theconversion reaction; and wherein the conversion reaction can comprisehydrogenation, hydrogenolysis, or hydrodeoxygenation. In the methodsdisclosed herein, the conversion reaction can convert a biomass-derivedmolecule to form a product. In the methods disclosed herein, thebiomass-derived molecule can be derived from lignocellulosic biomass,and the biomass-derived molecule can be selected from a saccharide, adehydrated saccharide, a halodehydrated saccharide, a dehydrated andpartially hydrogenated saccharide, or a hydrogenated saccharide, or acombination thereof. In the methods disclosed herein, the saccharide orthe dehydrated saccharide can be selected from monosaccharide,oligosaccharide, furfural, halofurfural, methyl furfural, furfurylalcohol, methyl furfuryl alcohol, (methoxymethyl)-methyl furfural,hydroxymethylfurfural, 2-methylfuran, dimethylfuran,2,5-bis(hydroxymethyl)furan, 5-hydroxymethyl-2-[(1-methylethoxy)methyl]furan, and 2-methyl-5[(1-methylmethoxy)methyl] furan,bis(1-methoxyethyxy)-methyl furan, tetrahydrofuran, or levoglucosenone,or a combination thereof. In the methods disclosed herein, thedehydrated and partially hydrogenated saccharide can be selected from1,2,6-hexanetriol, 1,2,5-pentanetriol, 1,2,4-butanetriol, 2,4-dihydroxybutanoic acid, or succinic acid, malic acid, maleic acid, or acombination thereof. In the methods disclosed herein, the hydrogenatedsaccharide can be selected from xylitol, mannitol, sorbitol, erythritol,arabitol, or galactitol, or a combination thereof. In the methodsdisclosed herein, the weight yield of the product can be at least 40%,45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, or 90%. In the methodsdisclosed herein, the selectivity to the product can be at least 40%,45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, or 90%.

In the methods disclosed herein, the method can comprise diluting2-butanol with a solvent, wherein the solvent can be inert in theconversion reaction. In the methods disclosed herein, the solvent cancomprise a C₄-C₁₈ hydrocarbon. In the methods disclosed herein, theC₄-C₁₈ hydrocarbon can be selected from hexane, cyclohexane, heptane,octane, decane, dodecane, or a combination thereof. In the methodsdisclosed herein, the method can further comprise catalyzing thedehydrogenation reaction and the conversion reaction with a catalyst. Inthe methods disclosed herein, catalyzing can be achieved using acopper-based catalyst, a Raney nickel-based catalyst, a metal containingorganosilica-based catalyst, or an iridium complex-based catalyst, or acombination thereof. In the methods disclosed herein, catalyzing can beachieved using a co-catalyst, an enhancer, or a promoter, or acombination thereof. In the methods disclosed herein, thedehydrogenation reaction and the conversion reaction can occur in onereaction vessel; or the dehydrogenation reaction and the conversionreaction can occur in more than one reactor vessels, wherein the morethan one reactor vessels are functionally connected either continuouslyor discontinuously.

In the methods disclosed herein, the conversion reaction can compriseconversion of furfural to 1,5-pentanediol. In the methods disclosedherein, the conversion of furfural to 1,5-pentanediol can comprise:contacting furfural with the hydrogen removed from the 2-butanol duringdehydrogenation in the presence of a first catalyst at a firsttemperature and a first pressure to yield furfuryl alcohol; andcontacting furfuryl alcohol with the hydrogen removed from the 2-butanolduring dehydrogenation in the presence of a second catalyst at a secondtemperature and a second pressure to yield 1,5-pentanediol; wherein thefirst catalyst and the second catalyst, the first temperature and thesecond temperature, and the first pressure and the second pressure arethe same or different; and wherein the dehydrogenation reaction and theconversion reaction occur in one reaction vessel, or wherein thedehydrogenation reaction and the conversion reaction occur in more thanone reactor vessels, wherein the more than one reactor vessels arefunctionally connected either continuously or discontinuously. In themethods disclosed herein, the first catalyst can be xCu-yMgO-zCr₂O₃,where x, y, and z are the amounts in terms of weight percent of Cu, MgO,and Cr₂O₃, respectively. In the methods disclosed herein, the conversionof furfural to 1,5-pentanediol can be achieved using a co-catalyst, anenhancer, or a promoter. In the methods disclosed herein, the firsttemperature can be less than 100, 110, 120, 130, 140, 150, 160, 170,180, 190, 200, 210, 220, 230, 250, or 250° C. In the methods disclosedherein, the molar ratio of 2-butanol to furfural can be 0.5, 1.0, 1.5,2.0, 2.5, 3.0, 3.5, 4.0, 4.5, 5.0, 5.5, 6.0, 6.5, 7.0, 7.5, 8.0, 8.5,9.0, 9.0, 9.5, or 10.0.

In the methods disclosed herein, the conversion reaction can compriseconversion of hydroxymethylfurfural to 1,6-hexanediol. In the methodsdisclosed herein, the conversion of hydroxymethylfurfural to1,6-hexanediol can comprise: contacting hydroxymethylfurfural with thehydrogen removed from the 2-butanol during dehydrogenation in thepresence of a first catalyst at a first temperature and a first pressureto yield bi-hydrodroxymethyl furan; contacting bi-hydrodroxymethyl furanwith the hydrogen removed from the 2-butanol during dehydrogenation inthe presence of a second catalyst at a second temperature and a secondpressure to yield hexanetriol; contacting hexanetriol with the hydrogenremoved from the 2-butanol during dehydrogenation in the presence of athird catalyst at a third temperature and a third pressure to yield1,6-hexanediol; wherein the first catalyst, the second catalyst, and thethird catalyst; the first temperature, the second temperature, and thethird temperature; and the first pressure, the second pressure, and thethird pressure are the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected either ordiscontinuously. In the methods disclosed herein, at least 40%, 45%,50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, or 90% of convertedhydroxymethylfurfural can be converted to 1,6-hexanediol. In the methodsdisclosed herein, the first catalyst can comprise a metal-containingorganosilica catalyst comprising one or more metal catalyst or aprecursor thereof and silica, wherein the metal catalyst or a precursorthereof is incorporated into a network of Si—O—Si bonds of the silica.In the methods disclosed herein, the catalyst can comprise one or moremetal catalyst or a precursor thereof and can comprise Cu, CuO,Cu₂Cr₂O₅, Pd, PdO, Pt, Rh, Ru, Co, Fe, or Ag, or a combination thereof.In the methods disclosed herein, the conversion of hydroxymethylfurfuralto 1,6-hexanediol can be achieved using a co-catalyst, an enhancer, or apromoter, or a combination thereof. In the methods disclosed herein, themethod can further comprise processing 1,6-hexanediol to produce acommercial product. In the methods disclosed herein, the commercialproduct can comprise a polymer, wherein the polymer can be selected frompolyester, polyurethane, polyamide, polycarbonate, polyacetate or epoxyresin, or a combination thereof.

In the methods disclosed herein, the conversion reaction can compriseconversion of 2,4-hydroxybutanoic acid to 1,4-butanediol. In the methodsdisclosed herein, the conversion of 2,4-hydroxybutanoic acid to1,4-butanediol can comprise: contacting 2,4-hydroxybutanoic acid withthe hydrogen removed from the 2-butanol during dehydrogenation in thepresence of a first catalyst at a first temperature and a first pressureto yield 1,2,4-butanetriol; and contacting 1,2,4-butanetriol with thehydrogen removed from the 2-butanol during dehydrogenation in thepresence of a second catalyst at a second temperature and a secondpressure to yield 1,4-butanediol; wherein the first catalyst and thesecond catalyst, the first temperature and the second temperature, andthe first pressure and the second pressure are the same or different;and wherein the dehydrogenation reaction and the conversion reactionoccur in one reaction vessel, or wherein the dehydrogenation reactionand the conversion reaction occur in more than one reactor vessels,wherein the more than one reactor vessels are functionally connectedeither continuously or discontinuously. In the methods disclosed herein,the conversion of 2,4-hydroxybutanoic acid to 1,4-butanediol can beachieved using a co-catalyst, an enhancer, or a promoter, or acombination thereof. In the methods disclosed herein, at least 40%, 45%,50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of 2-butanol can bedehydrogenated. In the methods disclosed herein, the percent weightyield of MEK from dehydrogenated 2-butanol can be at least 65%, 70%,75%, 80%, 85%, 90%, or 95%. In the methods disclosed herein, the methodcan not comprise adding formic acid, isopropanol, or gaseous molecularhydrogen from a source other than the hydrogen removed from the2-butanol during dehydrogenation. In the methods disclosed herein, theconversion reaction can convert a biomass-derived molecule to form aproduct.

Provided herein are processes to convert a biomass-derived molecule to aconversion product. The processes can comprise: using the conversionreaction to convert the biomass-derived molecule to the conversionproduct; wherein the conversion reaction can comprise hydrogenation,hydrogenolysis, or hydrodeoxygenation; and using a dehydrogenationreaction as a source of hydrogen for the conversion reaction. In theprocesses disclosed herein, the dehydrogenation reaction can comprisedehydrogenation of 2-butanol to 2-butanone. In the processes disclosedherein, at least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%,or 95% of 2-butanol can be dehydrogenated. In the processes disclosedherein, the percent weight yield of MEK from dehydrogenated 2-butanolcan be at least 65%, 70%, 75%, 80%, 85%, 90%, or 95%.

In the processes disclosed herein, the processes can further comprisediluting 2-butanol with a solvent, wherein the solvent can be inert inthe conversion reaction. In the processes disclosed herein, the solventcan comprise a C₄-C₁₈ hydrocarbon. In the processes disclosed herein,the C₄-C₁₈ hydrocarbon can be selected from hexane, cyclohexane,heptane, octane, decane, or dodecane, or a combination thereof. In theprocesses disclosed herein, the process can further comprise catalyzingthe dehydrogenation reaction and the conversion reaction with acatalyst. In the processes disclosed herein, catalyzing can be achievedusing a copper-based catalyst, a Raney nickel-based catalyst, a metalcontaining organosilica-based catalyst, or an iridium complex-basedcatalyst, or a combination thereof. In the processes disclosed herein,catalyzing can be achieved using a co-catalyst, an enhancer, or apromoter, or a combination thereof. In the processes disclosed herein,the dehydrogenation reaction and the conversion reaction can occur inone reaction vessel; or the dehydrogenation reaction and the conversionreaction can occur in more than one reactor vessels, wherein the morethan one reactor vessels are functionally connected either continuouslyor discontinuously. In the processes disclosed herein, the conversionreaction can be performed under an inert gas. In the processes disclosedherein, the inert gas can be nitrogen. In the processes disclosedherein, the conversion reaction can be performed under pressure. In theprocesses disclosed herein, the conversion reaction can be performedunder a pressure of 50, 100, 200, 300, 400, 500, 600, 700, 800, 900,1000, 1100, or 1200 psi. In the processes disclosed herein, theconversion reaction can be performed at a temperature of 50, 60, 70, 80,90, 100, 110, 120, 130, 140, 150, 160, 170, 180, 190, 200, 210, 220,230, 240, 250, 260, 270, 280, 290, or 300° C. In the processes disclosedherein, the conversion reaction can be performed for a time period of0.1, 0.5, 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18,19, 20, 21, 22, 23, or 24 hours.

In the processes disclosed herein, the biomass-derived molecule can bederived from lignocellulosic biomass. In the processes disclosed herein,the product can comprise at least 50 ppb, 60 ppb, 70 ppb, 80 ppb, 90ppb, 100 ppb, 110 ppb, 120 ppb, 130 ppb, 140 ppb, or 150 ppb of a markermolecule, and wherein the marker molecule can be selected from2-butanol, 2-butanone,5-[(1-methylpropoxy)methyl]-2-furancarboxaldehyde,5-hydroxymethyl-2-[(1-methylpropoxy) methyl] furan,2-methyl-5-[(1-methylpropoxy)methyl]furan, or2,5-[bis(1-methylpropoxy)-methyl] furan, or a combination thereof.

In the processes disclosed herein, the conversion reaction can compriseconversion of furfural to 1,5-pentanediol. In the processes disclosedherein, the conversion of furfural to 1,5-pentanediol can comprise:contacting furfural with the hydrogen removed during the dehydrogenationreaction in the presence of a first catalyst at a first temperature anda first pressure to yield furfuryl alcohol; and contacting furfurylalcohol with the hydrogen removed during the dehydrogenation reaction inthe presence of a second catalyst at a second temperature and a secondpressure to yield 1,5-pentanediol; wherein the first catalyst and thesecond catalyst, the first temperature and the second temperature, andthe first pressure and the second pressure can be the same or different;and wherein the dehydrogenation reaction and the conversion reaction canoccur in one reaction vessel, or wherein the dehydrogenation reactionand the conversion reaction can occur in more than one reactor vessels,wherein the more than one reactor vessels can be functionally connectedeither continuously or discontinuously.

In the processes disclosed herein, the conversion reaction can compriseconversion of hydroxymethylfurfural to 1,6-hexanediol. In the processesdisclosed herein, the conversion of hydroxymethylfurfural to1,6-hexanediol can comprise: contacting hydroxymethylfurfural with thehydrogen removed during the dehydrogenation reaction in the presence ofa first catalyst at a first temperature and a first pressure to yieldbi-hydrodroxymethyl furan; contacting bi-hydrodroxymethyl furan with thehydrogen removed during the dehydrogenation reaction in the presence ofa second catalyst at a second temperature and a second pressure to yieldhexanetriol; contacting hexanetriol with the hydrogen removed during thedehydrogenation reaction in the presence of a third catalyst at a thirdtemperature and a third pressure to yield 1,6-hexanediol; wherein thefirst catalyst, the second catalyst, and the third catalyst; the firsttemperature, the second temperature, and the third temperature; and thefirst pressure, the second pressure, and the third pressure can be thesame or different; and wherein the dehydrogenation reaction and theconversion reaction can occur in one reaction vessel, or wherein thedehydrogenation reaction and the conversion reaction can occur in morethan one reactor vessels, wherein the more than one reactor vessels arefunctionally connected either continuously or discontinuously.

In the processes disclosed herein, the conversion reaction can compriseconversion of 2,4-hydroxybutanoic acid to 1,4-butanediol. In theprocesses disclosed herein, the conversion of 2,4-hydroxybutanoic acidto 1,4-butanediol can comprise: contacting 2,4-hydroxybutanoic acid withthe hydrogen removed during the dehydrogenation reaction in the presenceof a first catalyst at a first temperature and a first pressure to yield1,2,4-butanetriol; and contacting 1,2,4-butanetriol with the hydrogenremoved during the dehydrogenation reaction in the presence of a secondcatalyst at a second temperature and a second pressure to yield1,4-butanediol; wherein the first catalyst and the second catalyst, thefirst temperature and the second temperature, and the first pressure andthe second pressure can be the same or different; and wherein thedehydrogenation reaction and the conversion reaction can occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction can occur in more than one reactor vessels, whereinthe more than one reactor vessels are functionally connected eithercontinuously or discontinuously.

In the processes disclosed herein, a process can convert abiomass-derived molecule to a conversion product, and the process cancomprise performing any of the methods disclosed herein.

Provided herein are systems configured to perform a process to convert abiomass-derived molecule to a conversion product. The processes cancomprise: using a conversion reaction to convert the biomass-derivedmolecule to the conversion product; wherein the conversion reaction cancomprise hydrogenation, hydrogenolysis, or hydrodeoxygenation; and usinga dehydrogenation reaction as a source of hydrogen for the conversionreaction. In the systems disclosed herein, the dehydrogenation reactioncan comprise dehydrogenation of 2-butanol to 2-butanone. In the systemsdisclosed herein, at least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%,85%, 90%, or 95% of 2-butanol can be dehydrogenated. In the systemsdisclosed herein, the percent weight yield of MEK from dehydrogenated2-butanol can be at least 65%, 70%, 75%, 80%, 85%, 90%, or 95%.

In the systems disclosed herein, the system can further comprisediluting 2-butanol with a solvent, wherein the solvent can be inert inthe conversion reaction. In the systems disclosed herein, the solventcan comprise a C₄-C₁₈ hydrocarbon. In the systems disclosed herein, theC₄-C₁₈ hydrocarbon can be selected from hexane, cyclohexane, heptane,octane, decane, or dodecane, or a combination thereof. In the systemsdisclosed herein, the system can further comprising catalyzing thedehydrogenation reaction and the conversion reaction with a catalyst. Inthe systems disclosed herein, catalyzing can be achieved using acopper-based catalyst, a Raney nickel-based catalyst, a metal containingorganosilica-based catalyst, or an iridium complex-based catalyst, or acombination thereof. In the systems disclosed herein, catalyzing can beachieved using a co-catalyst, an enhancer, or a promoter, or acombination thereof. In the systems disclosed herein, thedehydrogenation reaction and the conversion reaction can occur in onereaction vessel; or the dehydrogenation reaction and the conversionreaction can occur in more than one reactor vessels, wherein the morethan one reactor vessels are functionally connected either continuouslyor discontinuously.

In the systems disclosed herein, the conversion reaction can beperformed under an inert gas. In the systems disclosed herein, the inertgas can be nitrogen. In the systems disclosed herein, the conversionreaction can be performed under pressure. In the systems disclosedherein, the conversion reaction can be performed under a pressure of 50,100, 200, 300, 400, 500, 600, 700, 800, 900, 1000, 1100, or 1200 psi. Inthe systems disclosed herein, the conversion reaction can be performedat a temperature of 50, 60, 70, 80, 90, 100, 110, 120, 130, 140, 150,160, 170, 180, 190, 200, 210, 220, 230, 240, 250, 260, 270, 280, 290, or300° C. In the systems disclosed herein, the conversion reaction can beperformed for a time period of 0.1, 0.5, 1, 2, 3, 4, 5, 6, 7, 8, 9, 10,11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22, 23, or 24 hours. In thesystems disclosed herein, the biomass-derived molecule can be derivedfrom lignocellulosic biomass.

In the systems disclosed herein, the conversion reaction can compriseconversion of furfural to 1,5-pentanediol. In the systems disclosedherein, the conversion of furfural to 1,5-pentanediol can comprise:contacting furfural with the hydrogen removed during the dehydrogenationreaction in the presence of a first catalyst at a first temperature anda first pressure to yield furfuryl alcohol; and contacting furfurylalcohol with the hydrogen removed during the dehydrogenation reaction inthe presence of a second catalyst at a second temperature and a secondpressure to yield 1,5-pentanediol; wherein the first catalyst and thesecond catalyst, the first temperature and the second temperature, andthe first pressure and the second pressure are the same or different;and wherein the dehydrogenation reaction and the conversion reactionoccur in one reaction vessel, or wherein the dehydrogenation reactionand the conversion reaction occur in more than one reactor vessels,wherein the more than one reactor vessels are functionally connectedeither continuously or discontinuously.

In the systems disclosed herein, the conversion reaction can compriseconversion of hydroxymethylfurfural to 1,6-hexanediol. In the systemsdisclosed herein, the conversion of hydroxymethylfurfural to1,6-hexanediol can comprise: contacting hydroxymethylfurfural with thehydrogen removed during the dehydrogenation reaction in the presence ofa first catalyst at a first temperature and a first pressure to yieldbi-hydrodroxymethyl furan; contacting bi-hydrodroxymethyl furan with thehydrogen removed during the dehydrogenation reaction in the presence ofa second catalyst at a second temperature and a second pressure to yieldhexanetriol; contacting hexanetriol with the hydrogen removed during thedehydrogenation reaction in the presence of a third catalyst at a thirdtemperature and a third pressure to yield 1,6-hexanediol; wherein thefirst catalyst, the second catalyst, and the third catalyst; the firsttemperature, the second temperature, and the third temperature; and thefirst pressure, the second pressure, and the third pressure are the sameor different; and wherein the dehydrogenation reaction and theconversion reaction occur in one reaction vessel, or wherein thedehydrogenation reaction and the conversion reaction occur in more thanone reactor vessels, wherein the more than one reactor vessels arefunctionally connected either continuously or discontinuously.

In the systems disclosed herein, the conversion reaction can compriseconversion of 2,4-hydroxybutanoic acid to 1,4-butanediol. In the systemsdisclosed herein, the conversion of 2,4-hydroxybutanoic acid to1,4-butanediol can comprise: contacting 2,4-hydroxybutanoic acid withthe hydrogen removed during the dehydrogenation reaction in the presenceof a first catalyst at a first temperature and a first pressure to yield1,2,4-butanetriol; and contacting 1,2,4-butanetriol with the hydrogenremoved during the dehydrogenation reaction in the presence of a secondcatalyst at a second temperature and a second pressure to yield1,4-butanediol; wherein the first catalyst and the second catalyst, thefirst temperature and the second temperature, and the first pressure andthe second pressure are the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected eithercontinuously or discontinuously.

In the systems disclosed herein, the catalyst can comprise Pd, Pt, Rh,Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al,Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raney nickel,Raney nickel/Cu, Raney nickel/Ag, Raney nickel/Au, Raney nickel/Sn,Raney nickel/Pb, Raney nickel/Zn, Raney nickel/Cd, Raney nickel/In,Raney nickel/Ge, MnO, NiO, MgO, Ir, CpIr, CpIr-N-heterocyclic carbene,organosilica, organotitania, organoallumina, organozirconia, Pd—Si—O—Si,Pt—Si—O—Si, Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si,Ir—Si—O—Si, Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or acombination thereof. In the systems disclosed herein, catalyzing thedehydrogenation reaction and the conversion reaction can comprise usinga second catalyst, wherein the second catalyst can comprise Pd, Pt, Rh,Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al,Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raney nickel,Raney nickel/Cu, Raney nickel/Ag, Raney nickel/Au, Raney nickel/Sn,Raney nickel/Pb, Raney nickel/Zn, Raney nickel/Cd, Raney nickel/In,Raney nickel/Ge, MnO, NiO, MgO, Ir, CpIr, CpIr-N-heterocyclic carbene,organosilica, organotitania, organoallumina, organozirconia, Pd—Si—O—Si,Pt—Si—O—Si, Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si,Ir—Si—O—Si, Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or acombination thereof. In the systems disclosed herein, catalyzing thedehydrogenation reaction and the conversion reaction can furthercomprise using a promoter. In the systems disclosed herein, the promotercan comprise CaO. In the systems disclosed herein, the promoter cancomprise BaO. In the systems disclosed herein, the promoter can compriseZrO. In the systems disclosed herein, the promoter can comprise K₂O. Inthe systems disclosed herein, the promoter can comprise MgO. In thesystems disclosed herein, the method can further comprise diluting2-butanol with a solvent. In the systems disclosed herein, the solventcan comprise hexane. In the systems disclosed herein, the solvent cancomprise cyclohexane. In the systems disclosed herein, the solvent cancomprise heptane. In the systems disclosed herein, the solvent cancomprise octane. In the systems disclosed herein, the solvent cancomprise decane. In the systems disclosed herein, the solvent cancomprise dodecane. In the systems disclosed herein, the solvent cancomprise isoparaffinic fluids.

In the systems disclosed herein, a system can be configured to perform aprocess to convert a biomass-derived molecule to a conversion product,wherein the process can comprise any of the processes disclosed herein.

DESCRIPTION OF THE FIGURES

FIG. 1A shows a simplified flow scheme for the coupled dehydrogenationand conversion reactions.

FIG. 1B shows an alternative simplified flow scheme for the coupleddehydrogenation and conversion reactions.

FIG. 2A shows a simplified flow scheme for the conversion of furfural totetrahydrofuran (THF).

FIG. 2B shows an alternative simplified flow scheme for the conversionof furfural to THF.

FIG. 3A shows a simplified conversion of 5-(hydroxymethyl)furfural (HMF)to 1,2,6-hexanetriol (HTOL), and the consecutive conversion of HTOL to1,6-hexanediol (HDO).

FIG. 3B shows a simplified conversion of HMF to bi-hydroxymethyl furan(BHMF) and the consecutive reactions of BHMF to HTOL and HTOL to HDO.

DETAILED DESCRIPTION OF THE INVENTION

The present disclosure relates to methods, processes, and systems forutilizing the dehydrogenation of 2-butanol as a hydrogen source forhydrogen-consuming hydrogenation, hydrogenolysis, or hydrodeoxygenationreactions of biomass or biomass-derived molecules.

The present methods, processes, and systems can be applied universallyto any number of hydrogen accepting reactions known to those of skill inthe art. One of ordinary skill in the art could readily identifysuitable hydrogen accepting reactions for pairing with thedehydrogenation of 2-butanol to 2-butanone. In these reactions, thehydrogen produced by the dehydrogenation reaction acts as the hydrogendonor in the conversion reaction to which it is coupled.

Biomass is an alternative source for important chemicals currently madefrom petroleum derivatives, including, but not limited to, variousorganic acids, alcohols, polyols, as well as solvents such as benzene,toluene, xylene, and tetrahydrofuran (THF). Technologies to refine crudebiomass to pure products of lignin and hemicellulose and cellulosicsugars are currently being developed. The products of these processesare sugars and lignin, which can require additional chemical processingto chemically convert them to a wide array of useful chemicals that canbe used as substitutes for petrochemicals.

Notable steps of the chemical conversion of lignocellulosic-derivedmolecules involve the hydrogenation, hydrogenolysis, orhydrodeoxygenation of one or more chemical moieties of the molecule.Typically, these reactions are performed using isolated molecularhydrogen under high pressure of hydrogen gas, typically over 60 barpressure of hydrogen (870 Psi).

The methods, processes, and systems of the present disclosure areconducted under conditions that effect hydrogenation, hydrogenolysis, orhydrodeoxygenation. Specifically, the hydrogenation or catalytictransfer hydrogenation of biomass or biomass-derived molecules. Thecatalytic transfer hydrogenation of biomass or biomass-derived moleculesis initiated by the release of hydrogen from the hydrogen-donormaterial, 2-butanol. The conversion reactions are driven by the in situhydrogen generation from the dehydrogenation of 2-butanol. 2-butanol isdehydrogenated to MEK according to the reaction:

CH₃CH₂CH₃CHOH→CH₃CH₂CH₃CO+H₂

Any biomass or biomass-derived molecule that can undergo hydrogenation,hydrogenolysis, or hydrodeoxygenation can be converted according to thesystems, methods, and processes herein. Biomass can include, but is notlimited to, any lignocellulosic material. Lignocellulosic material caninclude, but is not limited to, materials comprising hemicellulose,cellulose, lignin, lignin derivatives, starch, oligosaccharides,monosaccharides, dehydrated saccharides, halodehydrated saccharides,dehydrated and partially hydrogenated saccharides, or hydrogenatedsaccharides. Lignocellulosic material can also include compositematerials that contain not only lignocellulosic polymers, but also awide variety of small amounts of lipophilic or amphiphilic compounds,e.g., fatty acids, rosin acids, phytosteroids, as well as proteins andash elements. Preferably, lignocellulosic material can be derived fromnon-food sources. Lignocellulosic materials are renewable sources forthe production of amino acids for feed and food supplements, monomersand polymers for the plastic industry, and renewable sources fordifferent types of fuels, polyol sugar substitutes (xylitol, sorbitol,manitols and the like), and numerous other chemicals that can besynthesized from C₅ and C₆ sugars.

A biomass or biomass-derived molecule that is converted through thecoupling of the dehydration of 2-butanol (2-BuOH) to MEK to theconversion reaction can be derived from refined hemicellulose orcellulose sugars. Refined hemicellulose or cellulose sugars can bederived from lignocellulosic material by processing and refiningprocesses, which generally comprises pretreatment, hemicellulose sugarextraction and purification, cellulose hydrolysis and cellulose sugarrefining, lignin processing and refining, and direct lignin extraction.Biomass-derived molecules derived from refining of hemicellulose andcellulose sugars include, but are not limited to furfural, halofurfural,methyl furfural, furfuryl alcohol, methyl furfuryl alcohol,(methoxymethyl)-methyl furfural, hydroxymethylfurfural, 2-methylfuran,dimethylfuran, 2,5-bis(hydroxymethyl)furan,5-hydroxymethyl-2-[(1-methylethoxy)methyl] furan, and2-methyl-5[(1-methylmethoxy)methyl] furan, bis(1-methoxyethyxy)-methylfuran, tetrahydrofuran, levoglucosenone, 1,2,6-hexanetriol,1,2,5-pentanetriol, 1,2,4-butanetriol, 2,4-dihydroxy butanoic acid,succinic acid, malic acid, or maleic acid.

As used herein, the terms percent weight yield, percent conversion,percent mole yield, theoretical yield, and percent selectivity aredefined according to Equations (I)-(V) below:

$\begin{matrix}{{\% \mspace{14mu} {Weight}\mspace{14mu} {Yield}} = {\frac{{Wt}\mspace{14mu} {of}\mspace{14mu} {product}}{{Wt}\mspace{14mu} {of}\mspace{14mu} {reactant}} \times 100}} & (I) \\{{\% \mspace{14mu} {Conversion}} = {\left( {1 - \frac{{{Wt}\mspace{14mu} {of}\mspace{14mu} {reactant}},g}{{{Wt}\mspace{14mu} {of}\mspace{14mu} {reactant}\mspace{14mu} {at}\mspace{14mu} t_{0}},g}} \right) \times 100}} & ({II}) \\{{\% \mspace{14mu} {Mole}\mspace{14mu} {yield}} = {\frac{{{Wt}\mspace{14mu} {of}\mspace{14mu} {product}},g}{{{Theoretical}\mspace{14mu} {wt}\mspace{14mu} {of}\mspace{14mu} {product}},g} \times 100}} & ({III}) \\{{{{Theoretical}\mspace{14mu} {yield}} = {\frac{{{Wt}\mspace{14mu} {of}\mspace{14mu} {reactant}},g}{{{Reactant}\mspace{14mu} {MW}},{g\text{/}{mol}}} \times {Product}\mspace{14mu} {MW}}},{g\text{/}{mol}}} & ({IV}) \\{{\% \mspace{14mu} {Selectivity}} = {\frac{\% \mspace{14mu} {Mole}\mspace{14mu} {yield}}{\% \mspace{14mu} {Conversion}} \times 100}} & (V)\end{matrix}$

The abbreviation “MEK” refers to methyl ethyl ketone. The terms “MEK,”“methyl ethyl ketone,” and “2-butanone” are used interchangeably.

As used herein, where the indefinite article “a” or “an” is used withrespect to a statement or description of the presence of a step in aprocess disclosed herein, unless the statement or description explicitlyprovides to the contrary, the use of such indefinite article does notlimit the presence of the step in the process to one in number. As usedherein, when an amount, concentration, or other value or parameter isgiven as either a range, preferred range, or a list of upper preferablevalues and lower preferable values, this is to be understood asspecifically disclosing all ranges formed from any pair of any upperrange limit or preferred value and any lower range limit or preferredvalue, regardless of whether ranges are separately disclosed.

Where a range of numerical values is recited herein, unless otherwisestated, the range is intended to include the endpoints thereof, and allintegers and fractions within the range. It is not intended that thescope of the invention be limited to the specific values recited whendefining a range.

As used herein, the terms “comprises,” “comprising,” “includes,”“including,” “has,” “having,” “contains,” or “containing,” or any othervariation thereof, are intended to cover a non-exclusive inclusion. Forexample, a composition, a mixture, process, method, article, orapparatus that comprises a list of elements is not necessarily limitedto only those elements but can include other elements not expresslylisted or inherent to such composition, mixture, process, method,article, or apparatus. Further, unless expressly stated to the contrary,“or” refers to an inclusive or and not to an exclusive or.

As used herein, the term “about” refers to variation in the reportednumerical quantity that can occur. The term “about” means within 10, 9,8, 7, 6, 5, 4, 3, 2, or 1% of the reported numerical value.

Systems for Producing MEK and a Conversion Product

The present systems can be applied universally to any number of hydrogenaccepting reactions known to those of skill in the art. One of ordinaryskill in the art could readily identify suitable hydrogen acceptingreactions for pairing with the dehydrogenation of 2-butanol to2-butanone. In these reactions, the hydrogen produced by thedehydrogenation reaction acts as the hydrogen donor in the conversionreaction to which it is coupled.

Provided herein are systems to convert a biomass or biomass-derivedmolecule to form a conversion product through the coupling of thedehydration of 2-butanol to MEK to the conversion reaction.Specifically, the hydrogen produced by the dehydrogenation of 2-butanolto MEK acts as the hydrogen donor in the conversion reaction.

A schematic diagram of an exemplary system for producing MEK and aconversion product is shown in FIG. 1A and FIG. 1B. In general, thesystems of FIG. 1A and FIG. 1B convert a biomass or biomass-derivedmolecule to form a conversion product through the coupling of thedehydration of 2-butanol (2-BuOH) to MEK to the conversion reaction.Specifically, the hydrogen produced by the dehydrogenation of 2-butanolto MEK acts as the hydrogen donor in the conversion reaction. Inaddition to hydrogen and MEK, the dehydrogenation reaction of 2-butanolcan produce, in smaller quantities, additional by-products. Suchby-products can include ethers formed by the condensation of 2-butanolwith the alcohol groups present on the reactants or reactionintermediates. For example, at least one of di-sec-butyl ether,5-[(1-methylpropoxy)methyl]-2-Furancarboxaldehyde,5-hydroxymethyl-2-[(1-methylpropoxy)methyl] furan,2-methyl-5-[(1-methylpropoxy)methyl]furan, or2,5-[bis(1-methylpropoxy)-methyl] furan can be formed as a by-product ofthe dehydrogenation reaction. These ethers can be hydrolyzed underappropriate reaction conditions to release 2-butanol and the otheralcohols, which are then converted to MEK and the target product.

In FIG. 1A, the dehydrogenation reaction and the conversion reactionoccur in the same reactor tank 100. The system has an input thatincorporates a biomass or biomass-derived molecule into the system. Abiomass or biomass-derived molecule is added to reactor tank 100 eithermechanically or via an input valve. The input of the biomass orbiomass-derived molecule can be batch wise or constant flow. The systemalso has an input that incorporates 2-butanol into the system. 2-butanolis added to reactor tank 100 either mechanically or via an input valve.The input of 2-butanol can be batch wise or constant flow. A catalystcan be introduced into reactor tank 100. The catalyst can comprise Pd,Pt, Rh, Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃,Cu—Fe—Al, Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raneynickel, Raney nickel/Cu, Raney nickel/Ag, Raney nickel/Au, Raneynickel/Sn, Raney nickel/Pb, Raney nickel/Zn, Raney nickel/Cd, Raneynickel/In, Raney nickel/Ge, MnO, NiO, MgO, Ir, CpIr, CpIr-N-heterocycliccarbene, organosilica, organotitania, organoallumina, organozirconia,Pd—Si—O—Si, Pt—Si—O—Si, Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si,RuSi—O—Si, Ir—Si—O—Si, Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si,or a combination thereof. A co-catalyst can also be introduced intoreactor tank 100. A promoter can also be introduced into reactor tank100. A solvent can also be introduced into reactor tank 100. Thecontents of reactor tank 100 are allowed to react for a sufficientamount of time and at appropriate reaction conditions to yield thedesired products. Upon sufficient dehydrogenation and conversion, thecontents of reactor 100 are directed to distillation unit 110, whereproduct separation occurs. Unreacted 2-butanol can be returned toreactor tank 100 for further reaction, while MEK and a conversionproduct are collected at the head. The percent weight yield of MEK from2-butanol can be at least about 65%, 70%, 75%, 80%, 85%, 90%, or 95%(wt/wt), or the percent weight yield of MEK from dehydrogenated2-butanol can be at least about 65%, 70%, 75%, 80%, 85%, 90%, or 95%.The conversion product stream can comprise at least about 50 ppb, 60ppb, 70 ppb, 80 ppb, 90 ppb, 100 ppb, 110 ppb, 120 ppb, 130 ppb, 140ppb, or 150 ppb of a marker molecule. The marker molecule can comprise2-butanol, 2-butanone, 5-[(1-methylpropoxy)methyl]-2-furancarboxaldehyde, 5-hydroxymethyl-2-[(1-methylpropoxy)methyl] furan, 2-methyl-5-[(1-methylpropoxy)methyl]furan, or2,5-[bis(1-methylpropoxy)-methyl] furan, or a combination thereof.

Alternatively, the dehydrogenation reaction and the conversion reactionoccur in separate reactor tanks. For example, in FIG. 1B, thedehydrogenation reaction occurs in reactor tank 120 and the conversionreaction occurs in reactor tank 130. The system has an input thatincorporates 2-butanol into the system. 2-butanol is added to reactortank 120 either mechanically or via an input valve. The input of2-butanol can be batch wise or constant flow. A catalyst can beintroduced into reactor tank 120. The catalyst can comprise Pd, Pt, Rh,Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al,Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raney nickel,Raney nickel/Cu, Raney nickel/Ag, Raney nickel/Au, Raney nickel/Sn,Raney nickel/Pb, Raney nickel/Zn, Raney nickel/Cd, Raney nickel/In,Raney nickel/Ge, MnO, NiO, MgO, Ir, CpIr, CpIr-N-heterocyclic carbene,organosilica, organotitania, organoallumina, organozirconia, Pd—Si—O—Si,Pt—Si—O—Si, Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si,Ir—Si—O—Si, Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or acombination thereof. A co-catalyst can also be introduced into reactortank 120. A promoter can also be introduced into reactor tank 120. Asolvent can also be introduced into reactor tank 120. The contents ofreactor tank 120 allowed to react for a sufficient amount of time and atappropriate reaction conditions to yield the desired products. Uponsufficient dehydrogenation, the products can be separated. Unreacted2-butanol can be separated, collected, and returned to reactor tank 120for further reaction. The products of reactor tank 120 comprise MEK andhydrogen. The percent weight yield of MEK from 2-butanol can be at leastabout 65%, 70%, 75%, 80%, 85%, 90%, or 95% (wt/wt), or the percentweight yield of MEK from dehydrogenated 2-butanol can be at least about65%, 70%, 75%, 80%, 85%, 90%, or 95%. Hydrogen produced by thedehydrogenation of 2-butanol is diverted to reactor tank 130. Reactortank 120 and reactor tank 130 are functionally connected either directlyor indirectly such that hydrogen produced by the dehydrogenation of2-butanol can be introduced to tank 130. The introduction of hydrogencan be controlled such that the rate of release of molecular hydrogeninto reactor tank 130 increases the yield of the conversion reaction toa desired product. For example, where mono-reduction is preferred overpoly-reduction of a biomass-derived molecule.

Further, the system of FIG. 2B has an input that incorporates a biomassor biomass-derived molecule into the system. A biomass orbiomass-derived molecule is added to reactor tank 130 eithermechanically or via an input valve. The input of a biomass orbiomass-derived molecule can be batch wise or constant flow. A catalystcan be introduced into reactor tank 130. A catalyst can comprise Pd, Pt,Rh, Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al,Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raney nickel,Raney nickel/Cu, Raney nickel/Ag, Raney nickel/Au, Raney nickel/Sn,Raney nickel/Pb, Raney nickel/Zn, Raney nickel/Cd, Raney nickel/In,Raney nickel/Ge, MnO, NiO, MgO, Ir, CpIr, CpIr-N-heterocyclic carbene,organosilica, organotitania, organoallumina, organozirconia, Pd—Si—O—Si,Pt—Si—O—Si, Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si,Ir—Si—O—Si, Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or acombination thereof. A co-catalyst can also be introduced into reactortank 130. A promoter can also be introduced into reactor tank 130. Asolvent can also be introduced into reactor tank 130. The contents ofreactor tank 130 are allowed to react for a sufficient amount of timeand at appropriate reaction conditions to yield the desired products.Upon sufficient conversion, the contents of reactor 130 are directed todistillation unit 140, where product separation occurs. The conversionproduct stream can comprise at least about 50 ppb, 60 ppb, 70 ppb, 80ppb, 90 ppb, 100 ppb, 110 ppb, 120 ppb, 130 ppb, 140 ppb, or 150 ppb ofa marker molecule. The marker molecule can comprise 2-butanol,2-butanone, 5-[(1-methylpropoxy)methyl]-2-furancarboxaldehyde,5-hydroxymethyl-2-[(1-methylpropoxy) methyl] furan,2-methyl-5-[(1-methylpropoxy)methyl]furan, or2,5-[bis(1-methylpropoxy)-methyl] furan, or a combination thereof.

As is illustrated in FIG. 1A and FIG. 1B, the dehydrogenation reactionand the conversion reaction can be conducted in the same reactor tank,or can be performed in separate reactor tanks that are functionallyconnected such that hydrogen produced by the dehydration of 2-butanol isintroduced to the reactor tank where the conversion reaction is carriedout. Reaction conditions are selected so as to optimize thedehydrogenation of 2-butanol to MEK and the conversion of the biomass orbiomass-derived molecule to the desired product, whether thedehydrogenation and conversion reactions occur in the same or separatetanks. Accordingly, the dehydrogenation of 2-butanol as disclosed hereincan occur in the same or in a separate reaction tank or under the sameor different reaction conditions of the conversion reaction unlessotherwise specified. Likewise, the conversion of a biomass orbiomass-derived molecule as disclosed herein can occur in either thesame or in a separate reaction tank or under the same or differentreaction conditions of the dehydrogenation reaction unless otherwisespecified.

Reaction conditions of the systems exemplified by FIG. 1A, FIG. 1B, FIG.2A, and FIG. 2B can be controlled using a reaction control unit operablyconnected to the system. The reaction control unit can include acomputer configured to receive input regarding the reaction parameters.The reaction parameters can include, but are not limited to, reactiontime, reaction temperature, reaction pressure, as well as the identity,quantity, and concentration of reactants and products. The reactioncontrol unit can use the variables of, for example, reactiontemperature, reaction pressure, and the identity, quantity, andconcentration of reactants and products at a particular time in order tocalculate appropriate changes to the reaction parameters and in order toeffect control of the reaction parameters.

Reaction conditions can be selected and controlled so as to optimize theyield of MEK from the dehydrogenation of 2-butanol. Specifically,reaction conditions can be selected and controlled such that at least40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of2-butanol is dehydrogenated. Reaction conditions can be selected andcontrolled such that at least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%,80%, 85%, 90%, or 95% of dehydrogenated 2-butanol yields 2-butanone.Reaction conditions can be selected and controlled such that the percentweight yield of MEK from 2-butanol is at least about 65%, 70%, 75%, 80%,85%, 90%, or 95% (wt/wt), or the percent weight yield of MEK fromdehydrogenated 2-butanol is at least about 65%, 70%, 75%, 80%, 85%, 90%,or 95%. Reaction conditions can be selected and controlled such that thecoupled dehydrogenation and conversion reactions have selectivity to adesired product greater than 40%, 50%, 60%, 70%, 80%, or 90%, and weightyield greater than 40%, 50%, 60%, 70%, 80%, or 90%.

The reaction control unit can be configured to control the input of2-butanol or a biomass or biomass-derived molecule such that the molarratio of 2-butanol to a biomass or biomass-derived molecule is about0.5, 1.0, 1.5, 2.0, 2.5, 3.0, 3.5, 4.0, 4.5, 5.0, 5.5, 6.0, 6.5, 7.0,7.5, 8.0, 8.5, 9.0, 9.0, 9.5, or 10.0. An inert gas can be used duringone or more of the reactions of this disclosure. The inert gas can beadded at room temperature. For example, the reaction control unit can beconfigured to introduce nitrogen at room temperature to pressure ofabout 50, 100, 200, 300, 400, 500, 600, 700, 800, 900, 1000, 1100, or1200 psi. Preferably, the reaction is performed under a pressure ofabout 200 to about 1200 psi. The reaction control unit can be configuredto control the reaction temperature so that it is less than about 300,290, 280, 270, 260, 250, 240, 230, 220, 210, 200, 190, 180, 170, 160,150, 140, 130, 120, 110, 100, 90, 80, 70, 60, 50, 40, 30, or 25° C. Thereaction control unit can be configured to control the reactiontemperature so that it is over about 50, 60, 70, 80, 90, 100, 110, 120,130, 140, 150, 160, 170, 180, 190, 200, 210, 220, 230, 240, 250, 260,270, 280, 290, or 300° C. The reaction control unit can also beconfigured to control the reaction temperature so that it is betweenabout 70 to about 300° C. or between about 180 to about 220° C. Thereaction control unit can be configured to control the reaction time sothat the reaction is carried out for less than about 0.1, 0.5, 1, 2, 3,4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, or 20 hours.The reaction control unit can be configured to control the reaction timeso that the reaction is carried out for at least about 0.1, 0.5, 1, 2,3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22,23, or 24 hours. The reaction control unit can also be configured tocontrol the reaction time so that the reaction is carried out forbetween about 2 to about 20 hours or between about 4 to about 10 hours.

The system can have an input that incorporates a solvent into thesystem. 2-butanol can be the sole solvent, or it can be diluted with anadditional solvent, where the additional solvent is inert in thereaction. The additional solvent can be a C₄-C₁₈ hydrocarbon. The rangeof C₄-C₁₈ includes individual components, such as C₄, C₅, C₆, C₇, C₈,C₉, C₁₀, C₁₁, C₁₂, C₁₃, C₁₄, C₁₅, C₁₆, C₁₇, C₁₈, or any sub-combinationsthereof, such as, but not limited to, C₆-C₁₂, C₅-C₁₇, C₆-C₁₆, C₇-C₁₅,C₈-C₁₄, or C₉-C₁₃. The solvent can contain 6, 7, 8, 9, 10, 11, or 12carbons. For example, suitable solvents include, but are not limited to,hexane, cyclohexane, heptane, octane, decane, dodecane, or a mixturethereof. Suitable solvents can also be commercial solvent mixturesincluding, but not limited to, isoparaffinic fluids (available fromExxonMobil). The additional solvent can be selected according to itsability to dissolve the reactants or the products, its boiling point,its availability, or price, or any other chemical or industrialconsideration.

A catalyst can be introduced into the system. Both the dehydrogenationand the conversion reaction can occur using a catalyst, whether theconversion reaction and the dehydrogenation reaction occur in the sameor separate reactor tanks Depending on the specific biomass orbiomass-derived molecules to be converted and the desired product orproducts, the catalysts used to catalyze the dehydrogenation reactioncan also be used to catalyze the conversion reaction. Alternatively, anadditional catalyst can be used to catalyze the conversion reaction.Also, catalysis can be enhanced by introducing a co-catalyst, promoter,enhancer, or a combination thereof.

The catalyst that is introduced into the system can affect theefficiency of the coupling of the dehydrogenation reaction to theconversion reaction. The suitability of a catalyst will vary dependingon the functional groups present on the biomass or biomass-derivedmolecule, and on the desired conversion product. Not all functionalgroups have the same reactivity towards conversion. Therefore, thefunctional groups present on the biomass or biomass-derived molecule canaffect the choice of the catalyst substrate structure, metal, orligands. The functional groups present on the biomass or biomass-derivedmolecule can also affect whether a co-catalyst, promoter, Brönsted orLewis acid or base, or solvents are introduced into the system. Acatalyst can be selected according to the structure of the biomass orbiomass-derived molecule, or according to other factors, such as itsactivity and selectivity, as well as its ability to be regenerated.Certain exemplary catalysts, co-catalysts, and promotors for use withthe dehydrogenation and conversion reactions are described below.Additional suitable catalysts, co-catalysts, and promoters can be knownin the art.

A suitable catalyst can contain a transition metal. For example, thecatalyst can comprise Pd, Pt, Rh, Ni, or Ru. A suitable catalyst cancomprise copper, which can include, but is not limited to, supportedcopper, copper oxide, and copper chromite catalysts. A suitable copperbased catalyst can comprise Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si,CuO/Al₂O₃, Cu—Fe—Al alloy, Cu—Zn—Al alloy, or Cu—Ni. Additionally, asuitable copper-based catalyst can have the formula xCu-yMgO-zCr₂O₃,where x, y, and z are the amounts in terms of weight percent of Cu, MgO,and Cr₂O₃, respectively. Specifically, the copper based catalyst canhave a Cu content of about 5 to about 50 weight percent, preferably ofabout 10 to about 25 weight percent; a Cr₂O₃ content of about 0 to about15 weight percent, preferably of about 1 to about 10 weight percent;where the balance is MgO.

A suitable catalyst can comprise a bimetallic component. For example,Ru, Au or lead-aluminum-borate compounds can be used as catalysts. Thecatalyst can be Raney nickel or a Raney nickel mixture comprising Raneynickel and about 0.1% to about 10% (wt/wt) of Cu, Ag, Au, Sn, Pb, Zn,Cd, In, or Ge. A suitable catalyst can comprise Ru, Au, or alead-aluminum-borate component, or the oxides of Mn, Ni, or Mg.

A suitable catalyst can comprise an Ir complex. The Ir complex can haveone or more cyclopentadienyl ligands, N-heterocyclic carbene (NHC)ligands, or a combination thereof. Specifically, the catalyst can be aCpIr or a CpIr-N-heterocyclic carbene complex.

A suitable catalyst can comprise a nanomaterial-based component. Such acatalyst can comprise, for example, palladium nanoparticles. Thenanomaterial can be dispersed in a medium, such as organosilica,organotitania, organoallumina, organozirconia, or a combination thereof.

A suitable catalyst can comprise a metal-containing organosilicacomponent. The metal-containing organosilica component can comprise oneor more metal catalysts or a metal catalyst precursor and silica, wherethe metal catalyst or a metal catalyst precursor is incorporated into anetwork of Si—O—Si bonds of silica. The metal-containing organosilicacatalyst can be a transition metal or a metal of Group 3A, Group 4A,Group 5A, or Group 6A of the periodic table. The metal catalyst or metalcatalyst precursor can comprise palladium, platinum, copper, copperoxide, copper chromite, ruthenium, iridium, silver, iron, cobalt,rhodium, or a combination thereof.

Any of the catalysts disclosed herein can be used with hexane. Any ofthe catalysts disclosed herein can be used with cyclohexane. Any of thecatalysts disclosed herein can be used with heptane. Any of thecatalysts disclosed herein can be used with octane. Any of the catalystsdisclosed herein can be used with decane. Any of the catalysts disclosedherein can be used with dodecane. Any of the catalysts disclosed hereincan be used with isoparaffinic fluids. Any of the catalysts disclosedherein can be used with a mixture comprising hexane, cyclohexane,heptane, octane, decane, dodecane, or isoparaffinic fluids.

The catalyzed reactions of the present disclosure can further comprise apromoter. The promoter can be incorporated into a reaction to, forexample, prevent catalyst fouling. Exemplary promoters include, but arenot limited to, CaO, BaO, ZrO, K₂O, MgO, or a combination thereof. Anyof the catalysts disclosed herein can be used with CaO. Any of thecatalysts disclosed herein can be used with Bao. Any of the catalystsdisclosed herein can be used with ZrO. Any of the catalysts disclosedherein can be used with K₂O. Any of the catalysts disclosed herein canbe used with MgO. Any of the catalysts disclosed herein can be used witha mixture comprising CaO, BaO, ZrO, K₂O, or MgO.

The systems disclosed herein can be used to perform any of the methodsor process disclosed herein. The systems disclosed herein can be used toconvert any biomass or biomass-derived molecule. For example, the systemcan be used to convert HMF to 1,6-hexanediol. The system can be used toconvert 2,4-hydroxybutanoic acid to 1,4-butanediol. The system can beused to convert furfural to 1,5-pentanediol.

Methods for Producing MEK and a Conversion Product

The present methods can be applied universally to any number of hydrogenaccepting reactions known to those of skill in the art. One of ordinaryskill in the art could readily identify suitable hydrogen acceptingreactions for pairing with the dehydrogenation of 2-butanol to2-butanone. In these reactions, the hydrogen produced by thedehydrogenation reaction acts as the hydrogen donor in the conversionreaction to which it is coupled.

Provided herein are methods to convert a biomass or biomass-derivedmolecule to form a conversion product through the coupling of thedehydration of 2-butanol to MEK to the conversion reaction.Specifically, the hydrogen produced by the dehydrogenation of 2-butanolto MEK acts as the hydrogen donor in the conversion reaction.

Provided herein are methods for using 2-butanol as the hydrogen sourcefor a conversion reaction. A method for using 2-butanol as the hydrogensource for a conversion reaction can comprise: dehydrogenating 2-butanolto yield 2-butanone; wherein hydrogen removed from the 2-butanol duringdehydrogenating is the hydrogen source for the conversion reaction; andwherein the conversion reaction comprises hydrogenation, hydrogenolysis,or hydrodeoxygenation. Preferably, the methods disclosed herein do notcomprise adding molecular hydrogen from an external source. Preferably,the methods disclosed herein do not comprise adding formic acid,isopropanol, or gaseous molecular hydrogen from a source other than thehydrogen removed from the 2-butanol during dehydrogenation.

The methods disclosed herein can comprise the conversion of a biomass orbiomass-derived molecule to form a conversion product, where in abiomass or biomass-derived molecule is defined as disclosed above. Thebiomass or biomass-derived molecule can be derived from lignocellulosicbiomass. The biomass or biomass-derived molecule can be selected from asaccharide, a dehydrated saccharide, a halodehydrated saccharide, adehydrated and partially hydrogenated saccharide, or a hydrogenatedsaccharide, or a combination thereof. The saccharide or the dehydratedsaccharide can be selected from monosaccharide, oligosaccharide,furfural, halofurfural, methyl furfural, furfuryl alcohol, methylfurfuryl alcohol, (methoxymethyl)-methyl furfural,hydroxymethylfurfural, 2-methylfuran, dimethylfuran,2,5-bis(hydroxymethyl)furan, 5-hydroxymethyl-2-[(1-methylethoxy)methyl]furan, and 2-methyl-5[(1-methylmethoxy)methyl] furan,bis(1-methoxyethyxy)-methyl furan, tetrahydrofuran, or levoglucosenone,or a combination thereof. The dehydrated and partially hydrogenatedsaccharide can be selected from 1,2,6-hexanetriol, 1,2,5-pentanetriol,1,2,4-butanetriol, 2,4-dihydroxy butanoic acid, or succinic acid, malicacid, maleic acid, or a combination thereof. The hydrogenated saccharidecan be selected from xylitol, mannitol, sorbitol, erythritol, arabitol,or galactitol, or a combination thereof.

The dehydrogenation reaction and the conversion can reaction occur inone reaction tank, or the dehydrogenation reaction and the conversionreaction can occur in separate reaction tanks Where the dehydrogenationreaction and the conversion reaction occur in separate reaction tanks,the reactor tanks are functionally connected either continuously ordiscontinuously.

Conditions of the dehydrogenation reaction and conditions of theconversion reaction can be selected in order to optimize the yield ofthe products of the reaction. The weight yield of the product of themethods herein can be at least about 40%, 45%, 50%, 55%, 60%, 65%, 70%,75%, 80%, 85%, or 90%. And the selectivity to the product of the methodsherein can be at least about 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%,80%, 85%, or 90%. At least about 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%,80%, 85%, 90%, or 95% of 2-butanol can be dehydrogenated. The percentweight yield of MEK from dehydrogenated 2-butanol can be at least about65%, 70%, 75%, 80%, 85%, 90%, or 95%.

The molar ratio of 2-butanol to furfural can be about 0.5, 1.0, 1.5,2.0, 2.5, 3.0, 3.5, 4.0, 4.5, 5.0, 5.5, 6.0, 6.5, 7.0, 7.5, 8.0, 8.5,9.0, 9.0, 9.5, or 10.0. Additionally, 2-butanol can be diluted with asolvent, and the solvent can be inert in the conversion reaction. Thesolvent can comprise a C₄-C₁₈ hydrocarbon. The range of C₄-C₁₈ includesindividual components, such as C₄, C₅, C₆, C₇, C₈, C₉, C₁₀, C₁₁, C₁₂,C₁₃, C₁₄, C₁₅, C₁₆, C₁₇, C₁₈, or any sub-combinations thereof, such as,but not limited to, C₆-C₁₂, C₅-C₁₇, C₆-C₁₆, C₇-C₁₅, C₈-C₁₄, or C₉-C₁₃.The solvent can contain 6, 7, 8, 9, 10, 11, or 12 carbons. For example,suitable solvents include, but are not limited to, hexane, cyclohexane,heptane, octane, decane, dodecane, or a mixture thereof. Suitablesolvents can also be commercial solvent mixtures including, but notlimited to, isoparaffinic fluids (available from ExxonMobil). Theadditional solvent can be selected according to its ability to dissolvethe reactants or the products, its boiling point, its availability, orprice, or any other chemical or industrial consideration.

The method can also comprise catalyzing the dehydrogenation reaction andthe conversion reaction with a catalyst. The catalyzing can be achievedusing a copper based catalyst, a Raney nickel based catalyst, a metalcontaining organosilica based catalyst, or an iridium complex basedcatalyst, or a combination thereof. The catalyzing can be achieved usinga co-catalyst, an enhancer, or a promoter, or a combination thereof.

Both the dehydrogenation and the conversion reaction can occur acatalyst, whether the conversion reaction and the dehydrogenationreaction occur in the same or separate reactor tanks Depending on thespecific biomass or biomass-derived molecules to be converted and thedesired product or products, the catalysts used to catalyze thedehydrogenation reaction can also be used to catalyze the conversionreaction. Alternatively, an additional catalyst can be used to catalyzethe conversion reaction. Also, catalysis can be enhanced by introducinga co-catalyst, promoter, enhancer, or a combination thereof.

The catalyst that is introduced into the reaction can affect theefficiency of the coupling of the dehydrogenation reaction to theconversion reaction. The suitability of a catalyst will vary dependingon the functional groups present on the biomass or biomass-derivedmolecule, and on the desired conversion product. Not all functionalgroups have the same reactivity towards conversion. Therefore, thefunctional groups present on the biomass or biomass-derived molecule canaffect the choice of the catalyst substrate structure, metal, orligands. The functional groups present on the biomass or biomass-derivedmolecule can also affect whether a co-catalyst, promoter, Brønsted orLewis acid or base, or solvents are introduced into the reaction. Acatalyst can be selected according to the structure of the biomass orbiomass-derived molecule, or according to other factors, such as itsactivity and selectivity, as well as its ability to be regenerated.Certain exemplary catalysts, co-catalysts, and promotors for use withthe dehydrogenation and conversion reactions are described below.Additional suitable catalysts, co-catalysts, and promoters can be knownin the art.

A suitable catalyst can contain a transition metal. For example, thecatalyst can comprise Pd, Pt, Rh, Ni, or Ru. A suitable catalyst cancomprise copper, which can include, but is not limited to, supportedcopper, copper oxide, and copper chromite catalysts. A suitable copperbased catalyst can comprise Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si,CuO/Al₂O₃, Cu—Fe—Al alloy, Cu—Zn—Al alloy, or Cu—Ni. Additionally, asuitable copper-based catalyst can have the formula xCu-yMgO-zCr₂O₃,where x, y, and z are the amounts in terms of weight percent of Cu, MgO,and Cr₂O₃, respectively. Specifically, the copper based catalyst canhave a Cu content of about 5 to about 50 weight percent, preferably ofabout 10 to about 25 weight percent; a Cr₂O₃ content of about 0 to about15 weight percent, preferably of about 1 to about 10 weight percent;where the balance is MgO.

A suitable catalyst can comprise a bimetallic component. For example,Ru, Au or lead-aluminum-borate compounds can be used as catalysts. Thecatalyst can be Raney nickel or a Raney nickel mixture comprising Raneynickel and about 0.1% to about 10% (wt/wt) of Cu, Ag, Au, Sn, Pb, Zn,Cd, In, or Ge. A suitable catalyst can comprise Ru, Au, or alead-aluminum-borate component, or the oxides of Mn, Ni, or Mg.

A suitable catalyst can comprise an Ir complex. The Ir complex can haveone or more cyclopentadienyl ligands, N-heterocyclic carbene (NHC)ligands, or a combination thereof. Specifically, the catalyst can be aCpIr or a CpIr-N-heterocyclic carbene complex.

A suitable catalyst can comprise a nanomaterial-based component. Such acatalyst can comprise, for example, palladium nanoparticles. Thenanomaterial can be dispersed in a medium, such as organosilica,organotitania, organoallumina, organozirconia, or a combination thereof.

A suitable catalyst can comprise a metal-containing organosilicacomponent. The metal-containing organosilica component can comprise oneor more metal catalysts or a metal catalyst precursor and silica, wherethe metal catalyst or a metal catalyst precursor is incorporated into anetwork of Si—O—Si bonds of silica. The metal-containing organosilicacatalyst can be a transition metal or a metal of Group 3A, Group 4A,Group 5A, or Group 6A of the periodic table. The metal catalyst or metalcatalyst precursor can comprise palladium, platinum, copper, copperoxide, copper chromite, ruthenium, iridium, silver, iron, cobalt,rhodium, or a combination thereof.

The catalyzed reactions of the present disclosure can further comprise apromoter. The promoter can be incorporated into a reaction to, forexample, prevent catalyst fouling. Exemplary promoters include, but arenot limited to, CaO, BaO, ZrO, K₂O, MgO, or a combination thereof. Anyof the catalysts disclosed herein can be used with CaO. Any of thecatalysts disclosed herein can be used with Bao. Any of the catalystsdisclosed herein can be used with ZrO. Any of the catalysts disclosedherein can be used with K₂O. Any of the catalysts disclosed herein canbe used with MgO. Any of the catalysts disclosed herein can be used witha mixture comprising CaO, BaO, ZrO, K₂O, or MgO.

The systems disclosed herein can be used to perform any of the methodsor process disclosed herein. The systems disclosed herein can be used toconvert any biomass or biomass-derived molecule. For example, the systemcan be used to convert HMF to 1,6-hexanediol. The system can be used toconvert 2,4-hydroxybutanoic acid to 1,4-butanediol. The system can beused to convert furfural to 1,5-pentanediol.

The conversion reaction of the methods herein can comprise theconversion of furfural to 1,5-pentanediol. The conversion of furfural to1,5-pentanediol can comprise contacting furfural with the hydrogenremoved from the 2-butanol during dehydrogenation using a first catalystat a first temperature and a first pressure to yield furfuryl alcohol;and contacting furfuryl alcohol with the hydrogen removed from the2-butanol during dehydrogenation using a second catalyst at a secondtemperature and a second pressure to yield 1,5-pentanediol; wherein thefirst catalyst and the second catalyst, the first temperature and thesecond temperature, and the first pressure and the second pressure canthe same or different; and wherein the dehydrogenation reaction and theconversion reaction occur in one reaction tank, or wherein thedehydrogenation reaction and the conversion reaction occur in more thanone reactor tanks, wherein the more than one reactor tanks arefunctionally connected either continuously or discontinuously. The firstcatalyst of the method for the conversion of furfural to 1,5-pentanediolcan be xCu-yMgO-zCr₂O₃, where x, y, and z are the amounts in terms ofweight percent of Cu, MgO, and Cr₂O₃, respectively. Specifically, thecopper based catalyst can have a Cu content of about 5 to about 50weight percent, preferably of about 10 to about 25 weight percent; aCr₂O₃ content of about 0 to about 15 weight percent, preferably of about1 to about 10 weight percent; where the balance is MgO. The conversionof furfural to 1,5-pentanediol can be achieved by also using aco-catalyst, an enhancer, or a promoter. The conversion reaction can beachieved by catalyzing the reaction using a catalyst, wherein thecatalyst can comprise any of the catalysts disclosed herein, or anyknown in the art. The first temperature of the method can be less thanabout 100, 110, 120, 130, 140, 150, 160, 170, 180, 190, 200, 210, 220,230, 250, or 250° C.

The conversion reaction of the methods herein can comprise theconversion of hydroxymethylfurfural to 1,6-hexanediol. The conversion ofhydroxymethylfurfural to 1,6-hexanediol can comprise contactinghydroxymethylfurfural with the hydrogen removed from the 2-butanolduring dehydrogenation using a first catalyst at a first temperature anda first pressure to yield bi-hydrodroxymethyl furan; contactingbi-hydrodroxymethyl furan with the hydrogen removed from the 2-butanolduring dehydrogenation using a second catalyst at a second temperatureand a second pressure to yield hexanetriol; contacting hexanetriol withthe hydrogen removed from the 2-butanol during dehydrogenation using athird catalyst at a third temperature and a third pressure to yield1,6-hexanediol; wherein the first catalyst, the second catalyst, and thethird catalyst; the first temperature, the second temperature, and thethird temperature; and the first pressure, the second pressure, and thethird pressure can the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction tank, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor tanks, wherein themore than one reactor tanks are functionally connected either ordiscontinuously. The conversion reaction can be achieved by catalyzingthe reaction using a catalyst, wherein the catalyst can comprise any ofthe catalysts disclosed herein, or any known in the art.

At least about 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, or 90%of converted hydroxymethylfurfural can be converted to 1,6-hexanediol.The first catalyst of the method can comprise a metal-containingorganosilica catalyst comprising one or more metal catalyst or aprecursor thereof and silica, wherein the metal catalyst or a precursorthereof is incorporated into a network of Si—O—Si bonds of the silica.The catalyst can comprise one or more metal catalyst or a precursorthereof and comprises Cu, CuO, Cu₂Cr₂O₅, Pd, PdO, Pt, Rh, Ru, Co, Fe, orAg, or a combination thereof. The conversion of hydroxymethylfurfural to1,6-hexanediol can be achieved using a co-catalyst, an enhancer, or apromoter, or a combination thereof. The methods disclosed herein cancomprise processing 1,6-hexanediol to produce a commercial product. Thecommercial product comprises a polymer, wherein the polymer is selectedfrom polyester, polyurethane, polyamide, polycarbonate, polyacetate orepoxy resin, or a combination thereof.

The conversion reaction of the methods herein can comprise conversion of2,4-hydroxybutanoic acid to 1,4-butanediol. The conversion of2,4-hydroxybutanoic acid to 1,4-butanediol can comprise contacting2,4-hydroxybutanoic acid with the hydrogen removed from the 2-butanolduring dehydrogenation using a first catalyst at a first temperature anda first pressure to yield 1,2,4-butanetriol; and contacting1,2,4-butanetriol with the hydrogen removed from the 2-butanol duringdehydrogenation using a second catalyst at a second temperature and asecond pressure to yield 1,4-butanediol; wherein the first catalyst andthe second catalyst, the first temperature and the second temperature,and the first pressure and the second pressure can the same ordifferent; and wherein the dehydrogenation reaction and the conversionreaction occur in one reaction tank, or wherein the dehydrogenationreaction and the conversion reaction occur in more than one reactortanks, wherein the more than one reactor tanks are functionallyconnected either continuously or discontinuously. The conversion of2,4-hydroxybutanoic acid to 1,4-butanediol can be achieved using aco-catalyst, an enhancer, or a promoter, or a combination thereof. Theconversion reaction can be achieved by catalyzing the reaction using acatalyst, wherein the catalyst can comprise any of the catalystsdisclosed herein, or any known in the art.

Processes for Producing MEK and a Conversion Product

The present processes can be applied universally to any number ofhydrogen accepting reactions known to those of skill in the art. One ofordinary skill in the art could readily identify suitable hydrogenaccepting reactions for pairing with the dehydrogenation of 2-butanol to2-butanone. In these reactions, the hydrogen produced by thedehydrogenation reaction acts as the hydrogen donor in the conversionreaction to which it is coupled.

Provided herein are processes to convert a biomass or biomass-derivedmolecule to form a conversion product through the coupling of thedehydration of 2-butanol to MEK to the conversion reaction.Specifically, the hydrogen produced by the dehydrogenation of 2-butanolto MEK acts as the hydrogen donor in the conversion reaction.

Provided herein are processes to convert a biomass or biomass-derivedmolecule to a conversion product. The process can comprise a conversionreaction to convert the biomass or biomass-derived molecule to theconversion product; wherein the conversion reaction compriseshydrogenation, hydrogenolysis, or hydrodeoxygenation; and using adehydrogenation reaction as a source of hydrogen for the conversionreaction. Optionally, does not comprise the addition of molecularhydrogen from an external source. Optionally, the process does notcomprise addition of formic acid, isopropanol, or gaseous molecularhydrogen from a source other than the hydrogen produced from thedehydrogenation reaction. The dehydrogenation reaction can comprise thedehydrogenation of 2-butanol to 2-butanone. At least about 40%, 45%,50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of 2-butanol can bedehydrogenated. The percent weight yield of MEK from dehydrogenated2-butanol can be at least about 65%, 70%, 75%, 80%, 85%, 90%, or 95%.The biomass or biomass-derived molecule converted according to theprocesses herein can be derived from lignocellulosic biomass.

The processes described herein can further comprise diluting 2-butanolwith a solvent, wherein the solvent is inert in the conversion reaction.The solvent can comprise a C₄-C₁₈ hydrocarbon. The C₄-C₁₈ hydrocarboncan be selected from hexane, cyclohexane, heptane, octane, decane, ordodecane, or a combination thereof. The solvent can comprise a C₄-C₁₈hydrocarbon. The range of C₄-C₁₈ includes individual components, such asC₄, C₅, C₆, C₇, C₈, C₉, C₁₀, C₁₁, C₁₂, C₁₃, C₁₄, C₁₅, C₁₆, C₁₇, C₁₈, orany sub-combinations thereof, such as, but not limited to, C₆-C₁₂,C₅-C₁₇, C₆-C₁₆, C₇-C₁₅, C₈-C₁₄, or C₉-C₁₃. The solvent can contain 6, 7,8, 9, 10, 11, or 12 carbons. For example, suitable solvents include, butare not limited to, hexane, cyclohexane, heptane, octane, decane,dodecane, or a mixture thereof. Suitable solvents can also be commercialsolvent mixtures including, but not limited to, isoparaffinic fluids(available from ExxonMobil). The additional solvent can be selectedaccording to its ability to dissolve the reactants or the products, itsboiling point, its availability, or price, or any other chemical orindustrial consideration.

The dehydrogenation reaction and the conversion reaction can occur inone reaction tank, or the dehydrogenation reaction and the conversionreaction can occur in more than one reactor tanks Where thedehydrogenation reaction and the conversion reaction occur in more thanone reactor tanks, the reactor tanks are functionally connected eithercontinuously or discontinuously.

The processes disclosed herein can further comprise catalyzing thedehydrogenation reaction and the conversion reaction with a catalyst.The conversion reaction can be achieved by catalyzing the reaction usinga catalyst, wherein the catalyst can comprise any of the catalystsdisclosed herein, or any known in the art. The catalyzing can beachieved using a copper based catalyst, a Raney nickel based catalyst, ametal containing organosilica based catalyst, or an iridium complexbased catalyst, or a combination thereof. The catalyzing can be achievedusing a co-catalyst, an enhancer, or a promoter, or a combinationthereof.

The catalyst that is introduced into the system can affect theefficiency of the coupling of the dehydrogenation reaction to theconversion reaction. The suitability of a catalyst will vary dependingon the functional groups present on the biomass or biomass-derivedmolecule, and on the desired conversion product. Not all functionalgroups have the same reactivity towards conversion. Therefore, thefunctional groups present on the biomass or biomass-derived molecule canaffect the choice of the catalyst substrate structure, metal, orligands. The functional groups present on the biomass or biomass-derivedmolecule can also affect whether a co-catalyst, promoter, Brønsted orLewis acid or base, or solvents are introduced into the system. Acatalyst can be selected according to the structure of the biomass orbiomass-derived molecule, or according to other factors, such as itsactivity and selectivity, as well as its ability to be regenerated.Certain exemplary catalysts, co-catalysts, and promotors for use withthe dehydrogenation and conversion reactions are described below.Additional suitable catalysts, co-catalysts, and promoters can be knownin the art.

A suitable catalyst can contain a transition metal. For example, thecatalyst can comprise Pd, Pt, Rh, Ni, or Ru. A suitable catalyst cancomprise copper, which can include, but is not limited to, supportedcopper, copper oxide, and copper chromite catalysts. A suitable copperbased catalyst can comprise Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si,CuO/Al₂O₃, Cu—Fe—Al alloy, Cu—Zn—Al alloy, or Cu—Ni. Additionally, asuitable copper-based catalyst can have the formula xCu-yMgO-zCr₂O₃,where x, y, and z are the amounts in terms of weight percent of Cu, MgO,and Cr₂O₃, respectively. Specifically, the copper based catalyst canhave a Cu content of about 5 to about 50 weight percent, preferably ofabout 10 to about 25 weight percent; a Cr₂O₃ content of about 0 to about15 weight percent, preferably of about 1 to about 10 weight percent;where the balance is MgO.

A suitable catalyst can comprise a bimetallic component. For example,Ru, Au or lead-aluminum-borate compounds can be used as catalysts. Thecatalyst can be Raney nickel or a Raney nickel mixture comprising Raneynickel and about 0.1% to about 10% (wt/wt) of Cu, Ag, Au, Sn, Pb, Zn,Cd, In, or Ge. A suitable catalyst can comprise Ru, Au, or alead-aluminum-borate component, or the oxides of Mn, Ni, or Mg.

A suitable catalyst can comprise an Ir complex. The Ir complex can haveone or more cyclopentadienyl ligands, N-heterocyclic carbene (NHC)ligands, or a combination thereof. Specifically, the catalyst can be aCpIr or a CpIr-N-heterocyclic carbene complex.

A suitable catalyst can comprise a nanomaterial-based component. Such acatalyst can comprise, for example, palladium nanoparticles. Thenanomaterial can be dispersed in a medium, such as organosilica,organotitania, organoallumina, organozirconia, or a combination thereof.

A suitable catalyst can comprise a metal-containing organosilicacomponent. The metal-containing organosilica component can comprise oneor more metal catalysts or a metal catalyst precursor and silica, wherethe metal catalyst or a metal catalyst precursor is incorporated into anetwork of Si—O—Si bonds of silica. The metal-containing organosilicacatalyst can be a transition metal or a metal of Group 3A, Group 4A,Group 5A, or Group 6A of the periodic table. The metal catalyst or metalcatalyst precursor can comprise palladium, platinum, copper, copperoxide, copper chromite, ruthenium, iridium, silver, iron, cobalt,rhodium, or a combination thereof.

The catalyzed reactions of the present disclosure can further comprise apromoter. The promoter can be incorporated into a reaction to, forexample, prevent catalyst fouling. Exemplary promoters include, but arenot limited to, CaO, BaO, ZrO, K₂O, MgO, or a combination thereof.

The conversion reaction can be performed under an inert gas. The inertgas can be nitrogen. The conversion reaction can be performed underpressure. The conversion reaction can be performed under a pressure ofabout 50, 100, 200, 300, 400, 500, 600, 700, 800, 900, 1000, 1100, or1200 psi. The conversion reaction can be performed at a temperature ofabout 50, 60, 70, 80, 90, 100, 110, 120, 130, 140, 150, 160, 170, 180,190, 200, 210, 220, 230, 240, 250, 260, 270, 280, 290, or 300° C. Theconversion reaction can be performed for a time period of about 0.1,0.5, 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19,20, 21, 22, 23, or 24 hours.

The product of the processes can comprise at least about 50 ppb, 60 ppb,70 ppb, 80 ppb, 90 ppb, 100 ppb, 110 ppb, 120 ppb, 130 ppb, 140 ppb, or150 ppb of a marker molecule, wherein the marker molecule can comprise2-butanol, 2-butanone, 5-[(1-methylpropoxy)methyl]-2-furancarboxaldehyde, 5-hydroxymethyl-2-[(1-methylpropoxy)methyl] furan, 2-methyl-5-[(1-methylpropoxy)methyl]furan, or2,5-[bis(1-methylpropoxy)-methyl] furan, or a combination thereof.

The processes can comprise the conversion of furfural to1,5-pentanediol. The conversion of furfural to 1,5-pentanediol cancomprise contacting furfural with the hydrogen removed during thedehydrogenation reaction using a first catalyst at a first temperatureand a first pressure to yield furfuryl alcohol; and contacting furfurylalcohol with the hydrogen removed during the dehydrogenation reactionusing a second catalyst at a second temperature and a second pressure toyield 1,5-pentanediol; wherein the first catalyst and the secondcatalyst, the first temperature and the second temperature, and thefirst pressure and the second pressure can the same or different; andwherein the dehydrogenation reaction and the conversion reaction occurin one reaction tank, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor tanks, wherein themore than one reactor tanks are functionally connected eithercontinuously or discontinuously.

The processes can comprise the conversion of hydroxymethylfurfural to1,6-hexanediol. The conversion of hydroxymethylfurfural to1,6-hexanediol can comprises contacting hydroxymethylfurfural with thehydrogen removed during the dehydrogenation reaction using a firstcatalyst at a first temperature and a first pressure to yieldbi-hydrodroxymethyl furan; contacting bi-hydrodroxymethyl furan with thehydrogen removed during the dehydrogenation reaction using a secondcatalyst at a second temperature and a second pressure to yieldhexanetriol; contacting hexanetriol with the hydrogen removed during thedehydrogenation reaction using a third catalyst at a third temperatureand a third pressure to yield 1,6-hexanediol; wherein the firstcatalyst, the second catalyst, and the third catalyst; the firsttemperature, the second temperature, and the third temperature; and thefirst pressure, the second pressure, and the third pressure can the sameor different; and wherein the dehydrogenation reaction and theconversion reaction occur in one reaction tank, or wherein thedehydrogenation reaction and the conversion reaction occur in more thanone reactor tanks, wherein the more than one reactor tanks arefunctionally connected either continuously or discontinuously.

The processes can comprise the conversion of 2,4-hydroxybutanoic acid to1,4-butanediol. The conversion of 2,4-hydroxybutanoic acid to1,4-butanediol can comprise contacting 2,4-hydroxybutanoic acid with thehydrogen removed during the dehydrogenation reaction using a firstcatalyst at a first temperature and a first pressure to yield1,2,4-butanetriol; and contacting 1,2,4-butanetriol with the hydrogenremoved during the dehydrogenation reaction using a second catalyst at asecond temperature and a second pressure to yield 1,4-butanediol;wherein the first catalyst and the second catalyst, the firsttemperature and the second temperature, and the first pressure and thesecond pressure can the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction tank, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor tanks, wherein themore than one reactor tanks are functionally connected eithercontinuously or discontinuously.

The processes disclosed herein can be used to perform any of the methodsdisclosed herein.

Conversion Reactions Using Donor Hydrogen Produced from theDehydrogenation of 2-Butanol

The present methods, processes, and systems can be applied universallyto any number of hydrogen accepting reactions known to those of skill inthe art. One of ordinary skill in the art could readily identifysuitable hydrogen accepting reactions for pairing with thedehydrogenation of 2-butanol to 2-butanone. In these reactions, thehydrogen produced by the dehydrogenation reaction acts as the hydrogendonor in the conversion reaction to which it is coupled.

As disclosed above, numerous biomass or biomass-derived molecules canundergo conversion reactions. Accordingly, numerous biomass orbiomass-derived molecules can be converted according to the methods,processes, and systems disclosed herein. Such biomass or biomass-derivedmolecules can be known in the art. The following sections providenon-limiting examples of the conversion of biomass or biomass-derivedmolecules by the coupling of the dehydrogenation of 2-butanol to2-butanone to the conversion reaction.

1. Conversion of Furfural

The dehydration of 2-butanol to MEK can be coupled to the conversion offurfural (furaldehyde) to various products. As discussed above, thereaction conditions can be selected and controlled such that at least40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of2-butanol is dehydrogenated. Reaction conditions can be selected andcontrolled such that at least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%,80%, 85%, 90%, or 95% of dehydrogenated 2-butanol yields 2-butanone.Reaction conditions can be selected and controlled such that the percentweight yield of MEK from 2-butanol is at least about 65%, 70%, 75%, 80%,85%, 90%, or 95% (wt/wt), or the percent weight yield of MEK fromdehydrogenated 2-butanol is at least about 65%, 70%, 75%, 80%, 85%, 90%,or 95%. Reaction conditions can be selected and controlled such that thecoupled dehydrogenation and conversion reactions have selectivity to adesired product greater than 40%, 50%, 60%, 70%, 80%, or 90%, and weightyield greater than 40%, 50%, 60%, 70%, 80%, or 90%. The overallconversion of 2-butanol can be less than 100%, 80%, 60%, or 50%, and themolar yield of the dehydrogenated 2-butanol to MEK can be greater than80%, 85%, 90%, or 95%.

Furfural can be derived from hemicellulose sugars via an acid-catalyzedconversion or an ionic liquid catalytic conversion. Furfural can undergomultiple conversions to a wide spectrum of high-value chemicals,including, but not limited to, 2-methyl furan, furfuryl alcohol,1,5-pentanediol, or tetrahydrofuran (THF).

Furfural can be decarbonylated to form furan. Furfural can also beconverted under catalytic reduction to tetrahydrofuran (THF).

FIG. 2A illustrates the conversion of furfural to THF in the liquidphase. Furfural can be introduced into the heated reactor 200 where itis decarbonylated to furan. A catalyst can be introduced into the heatedreactor 200. A catalyst can comprise Pd, Pt, Rh, Ni, Ru, Cu/Si,Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al, Cu—Zn—Al, Cu—Ni,Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raney nickel, Raney nickel/Cu,Raney nickel/Ag, Raney nickel/Au, Raney nickel/Sn, Raney nickel/Pb,Raney nickel/Zn, Raney nickel/Cd, Raney nickel/In, Raney nickel/Ge, MnO,NiO, MgO, Ir, CpIr, CpIr-N-heterocyclic carbene, organosilica,organotitania, organoallumina, organozirconia, Pd—Si—O—Si, Pt—Si—O—Si,Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si, Ir—Si—O—Si,Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or a combinationthereof. The products of the reaction in the heated reactor 200 enterthe distillation unit 210, where product separation occurs. Theunreacted furfural is condensed and can be returned to the heatedreactor for further reaction, while furan, CO or CO₂, and H₂ arecollected at the head. The stream can be contacted with base to removeCO₂. The products can be cooled via heat exchanger 220 and chilled tank230. Furan and 2-butanol are introduced into reactor tank 240. Acatalyst can be introduced into reactor tank 240. Any catalyst disclosedherein can be used, or any catalyst known in the art can be used. Acatalyst can comprise Pd, Pt, Rh, Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅,Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al, Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au,lead-aluminum-borate, Raney nickel, Raney nickel/Cu, Raney nickel/Ag,Raney nickel/Au, Raney nickel/Sn, Raney nickel/Pb, Raney nickel/Zn,Raney nickel/Cd, Raney nickel/In, Raney nickel/Ge, MnO, NiO, MgO, Ir,CpIr, CpIr-N-heterocyclic carbene, organosilica, organotitania,organoallumina, organozirconia, Pd—Si—O—Si, Pt—Si—O—Si, Cu—Si—O—Si,Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si, Ir—Si—O—Si, Ag—Si—O—Si,Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or a combination thereof. Aco-catalyst can also be introduced into reactor tank 240. A promoter canalso be introduced into reactor tank 240. The products produced by thecoupled dehydrogenation reaction and conversion reaction comprise MEKand THF.

FIG. 2B illustrates the conversion of furfural to THF in the gas phase.The reaction conditions for the reactions performed in the gas phase aresimilar to the reaction conditions for the reactions performed in theliquid phase. Fufural can be introduced into the gas phase reactor 260with steam where it is decarbonylated to furan. A catalyst can beintroduced into reactor 260. Any catalyst disclosed herein can be used,or any catalyst known in the art can be used. A catalyst can comprisePd, Pt, Rh, Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃,Cu—Fe—Al, Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raneynickel, Raney nickel/Cu, Raney nickel/Ag, Raney nickel/Au, Raneynickel/Sn, Raney nickel/Pb, Raney nickel/Zn, Raney nickel/Cd, Raneynickel/In, Raney nickel/Ge, MnO, NiO, MgO, Ir, CpIr, CpIr-N-heterocycliccarbene, organosilica, organotitania, organoallumina, organozirconia,Pd—Si—O—Si, Pt—Si—O—Si, Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si,RuSi—O—Si, Ir—Si—O—Si, Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si,or a combination thereof. The products of the reaction in the gas phasereactor 260 can be cooled via heat exchanger 270. Furan, CO or CO₂, andH₂ are collected at the head. CO₂ can be removed by the CO₂ scrubber280. Furan and 2-butanol are introduced into reactor tank 290 under thereaction conditions described herein. A catalyst can be introduced intoreactor tank 290. A catalyst can comprise Pd, Pt, Rh, Ni, Ru, Cu/Si,Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al, Cu—Zn—Al, Cu—Ni,Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raney nickel, Raney nickel/Cu,Raney nickel/Ag, Raney nickel/Au, Raney nickel/Sn, Raney nickel/Pb,Raney nickel/Zn, Raney nickel/Cd, Raney nickel/In, Raney nickel/Ge, MnO,NiO, MgO, Ir, CpIr, CpIr-N-heterocyclic carbene, organosilica,organotitania, organoallumina, organozirconia, Pd—Si—O—Si, Pt—Si—O—Si,Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si, Ir—Si—O—Si,Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or a combinationthereof. A co-catalyst can also be introduced into reactor tank 290. Apromoter can also be introduced into reactor tank 290. The productsproduced by the coupled dehydrogenation reaction and conversion reactioncomprise MEK and THF.

In the reactions illustrated by FIG. 2A and FIG. 2B, furfural can bedecarbonylated to furan in the liquid phase or the gas phase with theuse of a suitable catalyst. Any catalyst disclosed herein can be used,or any catalyst known in the art can be used. A catalyst can comprisePd, Pt, Rh, Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃,Cu—Fe—Al, Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au, lead-aluminum-borate, Raneynickel, Raney nickel/Cu, Raney nickel/Ag, Raney nickel/Au, Raneynickel/Sn, Raney nickel/Pb, Raney nickel/Zn, Raney nickel/Cd, Raneynickel/In, Raney nickel/Ge, MnO, NiO, MgO, Ir, CpIr, CpIr-N-heterocycliccarbene, organosilica, organotitania, organoallumina, organozirconia,Pd—Si—O—Si, Pt—Si—O—Si, Cu—Si—O—Si, Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si,RuSi—O—Si, Ir—Si—O—Si, Ag—Si—O—Si, Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si,or a combination thereof. Heterogeneous catalysts can be used in eitherphase. Catalysts known to catalyze the decarbonylation of furfural tofuran include, but are not limited to, Mn chromites, Zinc molibdate,copper molibdate, oxides of Zn, Cr, Mn, Al and their mixed oxides, Nialloy catalysts, Ni/C, Ni/Cr oxide, Raney Ni, Al—Zn—Fe catalysts, Pd,Pt, Rh, Ru or Mo supported over carbon, silica, alumina, or variouszeolites. A basic salt can be added as enhancer that extends catalystlife. Suitable salts include, but are not limited to, Na₂CO₃, K₂CO₃,Cs₂CO₃, and other alkali carbonates.

Furfural can undergo catalytic reduction to form furfuryl alcohol, andthrough a consecutive conversion, to 1,5-pentanediol. The conversionreactions can be performed using any catalyst disclosed herein or anycatalyst known in the art. The catalyst can comprise xCu-yMgO-zCr₂O₃,where x, y, and z are the amounts in terms of weight percent of Cu, MgO,and Cr₂O₃, respectively. Specifically, the copper-based catalyst canhave a Cu content of about 5 to about 50 weight percent, or of about 10to about 25 weight percent; a Cr₂O₃ content of about 0 to about 15weight percent, or of about 1 to about 10 weight percent; where thebalance is MgO. The reaction temperature can be less than 200° C. inorder to prevent undesired reactions, and thereby improve reactionselectivity.

Furfural can be reduced via catalytic reduction to form 2-methyl furan.Any catalyst disclosed herein can be used, or any catalyst known in theart can be used. The catalyst used to catalyze the reaction can containa palladium component. For example, palladium on activated carbon orpalladium on allumina can be used. Other palladium catalysts that can beused in this conversion reaction include, but are not limited to, PdCl₂and Pd₂(dba)₃. The catalyst for this conversion reaction can alsocomprise Pt, Ru, Cu, Rh, or a combination thereof. Preferably, Ru/C canbe used as the catalyst. The reaction temperature can be between about70 to about 250° C. or between about 100 to about 200° C. The reactioncan be carried out for a time between about 2 to about 20 hours orbetween about 4 to about 10 hours.

The resulting furan is hydrogenated either in liquid phase or in the gasphase using a hydrogenation catalysts. The source of hydrogen can be theH₂ released during the dehydrogenation of 2-butanol, or, additionally,from the H₂ released in the first stage.

2. Conversion of 5-(hydroxymethyl)furfural

The dehydration of 2-butanol to MEK can be coupled to the conversion of5-(hydroxymethyl)furfural (HMF) to various products. As discussed above,the reaction conditions can be selected and controlled such that atleast 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of2-butanol is dehydrogenated. Reaction conditions can be selected andcontrolled such that at least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%,80%, 85%, 90%, or 95% of dehydrogenated 2-butanol yields 2-butanone.Reaction conditions can be selected and controlled such that the percentweight yield of MEK from 2-butanol is at least about 65%, 70%, 75%, 80%,85%, 90%, or 95% (wt/wt), or the percent weight yield of MEK fromdehydrogenated 2-butanol is at least about 65%, 70%, 75%, 80%, 85%, 90%,or 95%. Reaction conditions can be selected and controlled such that thecoupled dehydrogenation and conversion reactions have selectivity to adesired product greater than 40%, 50%, 60%, 70%, 80%, or 90%, and weightyield greater than 40%, 50%, 60%, 70%, 80%, or 90%. The overallconversion of 2-butanol can be less than 100%, 80%, 60%, or 50%, and themolar yield of the dehydrogenated 2-butanol to MEK can be greater than80%, 85%, 90%, or 95%.

HMF can be converted in sequential reactions to produce 1,6-hexanediol(HDO). FIG. 3B provides a simplified illustration of the conversion ofHMF to HDO. HMF is first hydrogenated to bi-hydroxymethyl furan (BHMF).BHMF is then reacted through hydrogenation and ring opening to HTOL. Theintermediate formed during the conversion of BHMF, i.e., HTOL, can becontrolled by varying reaction conditions, such as, for example, the useof a catalyst. Finally, HTOL goes through catalytic hydregenolysis toform HDO. At least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%,90%, or 95% of the reacted HMF is fully converted to HDO. The conversionof HMF to HDO requires 5 equivalents of 2-butanol converting to MEK,according to the following reaction:

5C₄H₁₀O+C₆H₆O₃→5C₄H₈O+C₆H₁₄O₂+H₂O

Suitable catalysts that can be used during the conversion of HMF to HDOinclude, but are not limited to, Ru/C, Pt/C, Au/TiO₂. Any catalystdisclosed herein can be used, or any catalyst known in the art can beused. Additionally, the catalyst can be a metal catalyst selected frompalladium, iridium, platinum, ruthenium, nickel, rhodium, scandium,titanium, vanadium, chromium, manganese, iron, cobalt, copper, zinc,yttrium, zirconium, niobium, molybdenum, technetium, silver, cadmium,lanthanum, hafnium, tantalum, tungsten, rhenium, osmium, gold, ormercury. The temperature of the reaction can be selected to provideoptimized selectivity for a desired product, as well as a higher rate of2-butanol dehydrogenation. The temperature of reaction can be greaterthan about 150, 160, 170, 180, 190, or 200° C.

3. Conversion of Carboxylic Acids and Carboxylic Acid Derivatives

The dehydrogenation of 2-butanol to MEK can be coupled to the conversionof carboxylic acids and carboxylic acid derivatives to various products.As discussed above, the reaction conditions can be selected andcontrolled such that at least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%,80%, 85%, 90%, or 95% of 2-butanol is dehydrogenated. Reactionconditions can be selected and controlled such that at least 40%, 45%,50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of dehydrogenated2-butanol yields 2-butanone. Reaction conditions can be selected andcontrolled such that the percent weight yield of MEK from 2-butanol isat least about 65%, 70%, 75%, 80%, 85%, 90%, or 95% (wt/wt), or thepercent weight yield of MEK from dehydrogenated 2-butanol is at leastabout 65%, 70%, 75%, 80%, 85%, 90%, or 95%. Reaction conditions can beselected and controlled such that the coupled dehydrogenation andconversion reactions have selectivity to a desired product greater than40%, 50%, 60%, 70%, 80%, or 90%, and weight yield greater than 40%, 50%,60%, 70%, 80%, or 90%. The overall conversion of 2-butanol can be lessthan 100%, 80%, 60%, or 50%, and the molar yield of the dehydrogenated2-butanol to MEK can be greater than 80%, 85%, 90%, or 95%.

2,4-dihydroxy butanoic acid can be hydrogenated to 1,4-butanedioldirectly with a catalyst. Any catalyst disclosed herein can be used, orany catalyst known in the art can be used. Alternatively, 2,4-dihydroxybutanoic acid can be hydrogenated to 1,2,4-butanetriol, and, through aconsecutive reaction, to 1,4-butanediol.

The dehydrogenation of 2-butanol to MEK can be coupled to the conversionof 2-hydroxybutanedioic acid (malic acid) or butanedioic acid (succinicacid) to 1,4-butanediol.

Many other carboxylic acids and carboxylic acid derivatives can beconverted by coupling with the dehydrogenation of 2-butanediol to MEK.

4. Conversion of Levoglucosenone

The dehydrogenation of 2-butanol to MEK can be coupled to the conversionof levoglucosenone to produce various products. As discussed above, thereaction conditions can be selected and controlled such that at least40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of2-butanol is dehydrogenated. Reaction conditions can be selected andcontrolled such that at least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%,80%, 85%, 90%, or 95% of dehydrogenated 2-butanol yields 2-butanone.Reaction conditions can be selected and controlled such that the percentweight yield of MEK from 2-butanol is at least about 65%, 70%, 75%, 80%,85%, 90%, or 95% (wt/wt), or the percent weight yield of MEK fromdehydrogenated 2-butanol is at least about 65%, 70%, 75%, 80%, 85%, 90%,or 95%. Reaction conditions can be selected and controlled such that thecoupled dehydrogenation and conversion reactions have selectivity to adesired product greater than 40%, 50%, 60%, 70%, 80%, or 90%, and weightyield greater than 40%, 50%, 60%, 70%, 80%, or 90%. The overallconversion of 2-butanol can be less than 100%, 80%, 60%, or 50%, and themolar yield of the dehydrogenated 2-butanol to MEK can be greater than80%, 85%, 90%, or 95%.

For example, levoglucosenone can be hydrogenated to producelevoglucosanol, dihydrolevoglucosenone,1,6-anhydro-3,4-dideoxy-p-D-pyranose-2-one, 1,2,5,6-tetrahydroxyhexane,tetrahydro-2,5-furandimethanol, 1,2,6-hexanetriol,tetrahydro-2H-pyran-2-methanol,2-hydroxymethyl-5-hydroxytetrahydro-2H-pyran, tetrahydrofuran2,5-dimethanol, 2-hydroxymethyltetrahydropyran,1,2,5,6,-tetrahydroxyhexane, 1,2,5-hexanetriol,2-hydroxymethyl-5hydroxytetrahydropyran, 1,6-hexanediol, 1,2-hexanediol,1,2-cyclohexanediol, 1,5-hexanediol, 1-hexanol, 1-pentanol, or1,5-pentanediol.

The conversion reaction can be carried out under reaction conditions asdisclosed herein. Any catalyst disclosed herein can be used, or anycatalyst known in the art can be used.

Compositions of the Systems, Methods, and Process

Provided herein are compositions. A composition can comprise aconversion product. A composition can be produced by the processing of abiomass or biomass-derived molecule that is converted according to thesystems, methods, and processes disclosed herein. A composition cancomprise a commercial product. The commercial product can be produced byprocessing the conversion product. The conversion product can beproduced by the conversion of a biomass or biomass-derived moleculeaccording to the systems, methods, and processes disclosed herein.

The commercial product can comprise a polymer, where the polymer can beselected from polyester, polyurethane, polyamide, polycarbonate,polyacetate or epoxy resin, or a combination thereof. A product cancomprise at least about 50 ppb, 60 ppb, 70 ppb, 80 ppb, 90 ppb, 100 ppb,110 ppb, 120 ppb, 130 ppb, 140 ppb, or 150 ppb of a marker molecule,wherein the marker molecule can comprise 2-butanol, 2-butanone,5-[(1-methylpropoxy) methyl]-2-furancarboxaldehyde,5-hydroxymethyl-2-[(1-methylpropoxy) methyl] furan,2-methyl-5-[(1-methylpropoxy)methyl]furan, or2,5-[bis(1-methylpropoxy)-methyl] furan, or a combination thereof.

EXAMPLES

It is understood that the examples and embodiments described herein arefor illustrative purposes only and are not intended to limit the scopeof the claimed invention. It is also understood that variousmodifications or changes in light the examples and embodiments describedherein will be suggested to persons skilled in the art and are to beincluded within the spirit and purview of this application and scope ofthe appended claims. All publications, patents, and patent applicationscited herein are hereby incorporated by reference in their entirety forall purposes.

Example 1 Conversion of Furan to THF

This example describes the coupling of 2-butanol dehydrogenation withthe conversion of furan to THF.

Furan was added to 2-butanol and dodecane in a 50 mL stirred Hastelloyreactor (Autoclave Engineering EZE-Seal). Copper chromite and Ni/silicacatalysts were used to catalyze the reaction. Nitrogen was used to flushand pressurize the reactor to 200 psi. The mixture was then heated to160 to 220° C. for 4 to 20 hours in a pressure reactor. After 4 hours,the reactor was cooled in an ice-water bath before opening. Theresulting product was analyzed by gas chromatography. The results aresummarized in Table 1.

TABLE 1 Hydrogenation of furan to THF with coupled de-hydrogenation of2-butanol to MEK Conditions Pressure, Reactants, g Products. g Ref T° C.hours Psi Ni/Si Cu2Cr2O5 Dodecane 2-BuOH Furan 2-BuOH MEK Furan 270114208 4 450 0.15 0.22 10.02 9.88 1.99 4.53 3.79 0.15 280214 219 4 626 0.720.69 11.97 11.87 3.98 2.43 8.32 0.54 060314 165 6 335 0.52 0.43 9.8910.75 4.22 8.64 2.02 2.85 080314 170 4.5 125 0.93 0.96 10.91 9.79 4.015.36 4.32 2.03 Products. g Furfuryl Dimethyl Converstion, % WeightYield, % Selectivity, % Ref THF alcohol furan 2-BuOH furan MEK THF MEKTHF 270114 0.98 0.10 0.07 54 92 38 49 73 50 280214 1.51 0.44 0.14 80 8770 38 91 41 060314 0.39 0.05 0.06 20 33 19 9 99 27 080314 1.02 0.22 0.0045 49 44 25 100 49

Example 2 Conversion Octene to Octane

This example describes the coupling of 2-butanol dehydrogenation withthe conversion of octene to octane.

Experiments are conducted to evaluate the efficiency of multipleorganosilica catalysts for the dehydrogenation of 2-butanol to MEK byusing octene as a reactant. The catalysts tested are Cu/SiO₂ (4.7%(wt/wt) Cu), CuO/SiO₂ (11.9% (wt/wt) CuO), Cu₂Cr₂O₅/SiO₂ (6% (wt/wt) Cuand 5.1% (wt/wt) Cr), and Pd/SiO₂. All catalysts are provided bySiliCycle Inc, Quebec City, Canada. To evaluate the recyclability of thecatalyst, the washed and dried catalyst is tested in repeated reactions.

The experiments are carried out in a 160 mL PARR Series 5500 HighPressure Compact Laboratory Reactor. The reactor is loaded with 30 g of100-50% 2-butanol/dodecane, 1.5 g octene, and 0.17 g catalyst. Nitrogenis added to yield pressures ranging from between 200 to 400 psi at roomtemperature. The reactions are conducted at multiple temperatures, whichrange from 180 to 240° C. The reaction time is controlled, and thereactions are conducted for multiple time periods, ranging from 4 to 24hours.

Samples of the liquid phase are analyzed by gas chromatography in orderto determine the concentration of 2-butanol, MEK, octene, and octane, aswell as to identify and quantify any other products formed in thereaction. The liquid phase is analyzed by inductively coupled plasmatechniques to detect leached metal.

The liquid phase is filtered at the end of the reaction to collect thesolid catalyst. At least 80% of the 2-butanol is converted to MEK, whilehydrogenating octene to octane.

Example 3 Conversion of HMF to HDO

This example describes the coupling of 2-butanol dehydrogenation withthe conversion of HMF to HDO.

Experiments are conducted to evaluate the efficacy of supported metalcatalysts for the catalytic conversion of HMF to HDO. The catalyststested are Cu/SiO₂ (4.7% (wt/wt) Cu), CuO/SiO₂ (11.9% (wt/wt) CuO),Cu₂Cr₂O₅/SiO₂ (6% (wt/wt) Cu and 5.1% (wt/wt) Cr), and Pd/SiO₂, as wellas a combination of a copper-based catalyst and a palladium-basedcatalyst. All catalysts are provided by SiliCycle Inc, Quebec City,Canada. To evaluate the recyclability of the catalyst, the washed anddried catalyst is tested in repeated reactions.

The reactions are carried out in a 160 mL PARR Series 5500 High PressureCompact Laboratory Reactor. The reactor is loaded with 30 g of 100-50%2-butanol/dodecane, 1.5 g octene, and 0.17 g catalyst. Nitrogen is addedto pressures ranging from between 200 to 400 psi at room temperature.The reactions are conducted at multiple temperatures, which range from180 to 240° C. The reaction time is controlled, and the reactions areconducted for multiple time periods, ranging from 4 to 24 hours.

Samples of the liquid phase are analyzed by gas chromatography todetermine the concentration of 2-butanol, MEK, HMF, BHMF,1,2,6-hexanetriol, and HDO, as well as to identify and quantify anyother intermediates or products formed in the reaction. The liquid phaseis analyzed by inductively coupled plasma techniques to detect leachedmetal.

The liquid phase is filtered at the end of the reaction to collect thesolid catalyst. At least 80% of the 2-butanol is converted to MEK, whilehydrogenating HMF to HDO.

What is claimed is:
 1. A method for using 2-butanol as the hydrogensource for a conversion reaction, the method comprising: dehydrogenating2-butanol to yield 2-butanone; wherein hydrogen removed from the2-butanol during dehydrogenating is the hydrogen source for theconversion reaction; and wherein the conversion reaction compriseshydrogenation, hydrogenolysis, or hydrodeoxygenation.
 2. The method ofclaim 1, wherein the conversion reaction converts a biomass-derivedmolecule to form a product.
 3. The method of claim 2, wherein thebiomass-derived molecule is derived from lignocellulosic biomass, andwherein the biomass-derived molecule is selected from a saccharide, adehydrated saccharide, a halodehydrated saccharide, a dehydrated andpartially hydrogenated saccharide, or a hydrogenated saccharide, or acombination thereof.
 4. The method of claim 3, wherein the saccharide orthe dehydrated saccharide is selected from monosaccharide,oligosaccharide, furfural, halofurfural, methyl furfural, furfurylalcohol, methyl furfuryl alcohol, (methoxymethyl)-methyl furfural,hydroxymethylfurfural, 2-methylfuran, dimethylfuran,2,5-bis(hydroxymethyl)furan, 5-hydroxymethyl-2-[(1-methylethoxy)methyl]furan, and 2-methyl-5[(1-methylmethoxy)methyl] furan,bis(1-methoxyethoxy)-methyl furan, tetrahydrofuran, or levoglucosenone,or a combination thereof.
 5. The method of claim 3, wherein thedehydrated and partially hydrogenated saccharide is selected from1,2,6-hexanetriol, 1,2,5-pentanetriol, 1,2,4-butanetriol, 2,4-dihydroxybutanoic acid, or succinic acid, malic acid, maleic acid, or acombination thereof.
 6. The method of claim 3, wherein the hydrogenatedsaccharide is selected from xylitol, mannitol, sorbitol, erythritol,arabitol, or galactitol, or a combination thereof.
 7. The method ofclaim 2, wherein the weight yield of the product is at least 40%, 45%,50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, or 90%.
 8. The method of claim2, wherein the selectivity to the product is at least 40%, 45%, 50%,55%, 60%, 65%, 70%, 75%, 80%, 85%, or 90%.
 9. The method of claim 1,further comprising diluting 2-butanol with a solvent, wherein thesolvent is inert in the conversion reaction.
 10. The method of claim 9,wherein the solvent comprises a C₄-C₁₈ hydrocarbon.
 11. The method ofclaim 10, wherein the C₄-C₁₈ hydrocarbon is selected from hexane,cyclohexane, heptane, octane, decane, dodecane, or a combinationthereof.
 12. The method of claim 1, further comprising catalyzing thedehydrogenation reaction and the conversion reaction with a catalyst.13. The method of claim 12, wherein catalyzing is achieved using acopper-based catalyst, a Raney nickel-based catalyst, a metal containingorganosilica-based catalyst, or an iridium complex-based catalyst, or acombination thereof.
 14. The method of claim 12, wherein catalyzing isachieved using a co-catalyst, an enhancer, or a promoter, or acombination thereof.
 15. The method of claim 1, wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel; or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected eithercontinuously or discontinuously.
 16. The method of claim 1, wherein theconversion reaction comprises conversion of furfural to 1,5-pentanediol.17. The method of claim 16, wherein the conversion of furfural to1,5-pentanediol comprises: contacting furfural with the hydrogen removedfrom the 2-butanol during dehydrogenation in the presence of a firstcatalyst at a first temperature and a first pressure to yield furfurylalcohol; and contacting furfuryl alcohol with the hydrogen removed fromthe 2-butanol during dehydrogenation in the presence of a secondcatalyst at a second temperature and a second pressure to yield1,5-pentanediol; wherein the first catalyst and the second catalyst, thefirst temperature and the second temperature, and the first pressure andthe second pressure are the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected eithercontinuously or discontinuously.
 18. The method of claim 17, wherein thefirst catalyst is xCu-yMgO-zCr₂O₃, where x, y, and z are the amounts interms of weight percent of Cu, MgO, and Cr₂O₃, respectively.
 19. Themethod of claim 17, wherein the conversion of furfural to1,5-pentanediol is achieved using a co-catalyst, an enhancer, or apromoter.
 20. The method of claim 17, wherein the first temperature isless than 100, 110, 120, 130, 140, 150, 160, 170, 180, 190, 200, 210,220, 230, 250, or 250° C.
 21. The method of claim 17, wherein the molarratio of 2-butanol to furfural is 0.5, 1.0, 1.5, 2.0, 2.5, 3.0, 3.5,4.0, 4.5, 5.0, 5.5, 6.0, 6.5, 7.0, 7.5, 8.0, 8.5, 9.0, 9.0, 9.5, or10.0.
 22. The method of claim 1, wherein the conversion reactioncomprises conversion of hydroxymethylfurfural to 1,6-hexanediol.
 23. Themethod of claim 22, wherein the conversion of hydroxymethylfurfural to1,6-hexanediol comprises: contacting hydroxymethylfurfural with thehydrogen removed from the 2-butanol during dehydrogenation in thepresence of a first catalyst at a first temperature and a first pressureto yield bi-hydrodroxymethyl furan; contacting bi-hydrodroxymethyl furanwith the hydrogen removed from the 2-butanol during dehydrogenation inthe presence of a second catalyst at a second temperature and a secondpressure to yield hexanetriol; contacting hexanetriol with the hydrogenremoved from the 2-butanol during dehydrogenation in the presence of athird catalyst at a third temperature and a third pressure to yield1,6-hexanediol; wherein the first catalyst, the second catalyst, and thethird catalyst; the first temperature, the second temperature, and thethird temperature; and the first pressure, the second pressure, and thethird pressure are the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected either ordiscontinuously.
 24. The method of claim 22 or 23, wherein at least 40%,45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, or 90% of convertedhydroxymethylfurfural is converted to 1,6-hexanediol.
 25. The method ofclaim 23, wherein the first catalyst comprises a metal-containingorganosilica catalyst comprising one or more metal catalyst or aprecursor thereof and silica, wherein the metal catalyst or a precursorthereof is incorporated into a network of Si—O—Si bonds of the silica.26. The method of claim 25, wherein the catalyst comprises one or moremetal catalyst or a precursor thereof and comprises Cu, CuO, Cu₂Cr₂O₅,Pd, PdO, Pt, Rh, Ru, Co, Fe, or Ag, or a combination thereof.
 27. Themethod of claim 23, wherein the conversion of hydroxymethylfurfural to1,6-hexanediol is achieved using a co-catalyst, an enhancer, or apromoter, or a combination thereof.
 28. The method of claim 22 or 23,further comprising processing 1,6-hexanediol to produce a commercialproduct.
 29. The method of claim 28, wherein the commercial productcomprises a polymer, wherein the polymer is selected from polyester,polyurethane, polyamide, polycarbonate, polyacetate or epoxy resin, or acombination thereof.
 30. The method of claim 1, wherein the conversionreaction comprises conversion of 2,4-hydroxybutanoic acid to1,4-butanediol.
 31. The method of claim 30, wherein the conversion of2,4-hydroxybutanoic acid to 1,4-butanediol comprises: contacting2,4-hydroxybutanoic acid with the hydrogen removed from the 2-butanolduring dehydrogenation in the presence of a first catalyst at a firsttemperature and a first pressure to yield 1,2,4-butanetriol; andcontacting 1,2,4-butanetriol with the hydrogen removed from the2-butanol during dehydrogenation in the presence of a second catalyst ata second temperature and a second pressure to yield 1,4-butanediol;wherein the first catalyst and the second catalyst, the firsttemperature and the second temperature, and the first pressure and thesecond pressure are the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected eithercontinuously or discontinuously.
 32. The method of claim 31, wherein theconversion of 2,4-hydroxybutanoic acid to 1,4-butanediol is achievedusing a co-catalyst, an enhancer, or a promoter, or a combinationthereof.
 33. The method of claim 1, 16, 17, 22, 23, 30, or 31, whereinat least 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95%of 2-butanol is dehydrogenated.
 34. The method of claim 33, wherein thepercent weight yield of MEK from dehydrogenated 2-butanol is at least65%, 70%, 75%, 80%, 85%, 90%, or 95%.
 35. The method of claim 1, 16, 17,22, 23, 30, or 31, wherein the method does not comprise adding formicacid, isopropanol, or gaseous molecular hydrogen from a source otherthan the hydrogen removed from the 2-butanol during dehydrogenation. 36.The method of claim 1, 16, 17, 22, 23, 30, or 31, wherein the conversionreaction converts a biomass-derived molecule to form a product.
 37. Aprocess to convert a biomass-derived molecule to a conversion product,the process comprising: using the conversion reaction to convert thebiomass-derived molecule to the conversion product; wherein theconversion reaction comprises hydrogenation, hydrogenolysis, orhydrodeoxygenation; and using a dehydrogenation reaction as a source ofhydrogen for the conversion reaction.
 38. The process of claim 37,wherein the dehydrogenation reaction comprises dehydrogenation of2-butanol to 2-butanone.
 39. The process of claim 37, wherein at least40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of2-butanol is dehydrogenated.
 40. The process of claim 39, the percentweight yield of MEK from dehydrogenated 2-butanol is at least 65%, 70%,75%, 80%, 85%, 90%, or 95%.
 41. The process of claim 38, furthercomprising diluting 2-butanol with a solvent, wherein the solvent isinert in the conversion reaction.
 42. The process of claim 41, whereinthe solvent comprises a C₄-C₁₈ hydrocarbon.
 43. The process of claim 42,wherein the C₄-C₁₈ hydrocarbon is selected from hexane, cyclohexane,heptane, octane, decane, or dodecane, or a combination thereof.
 44. Theprocess of claim 37, further comprising catalyzing the dehydrogenationreaction and the conversion reaction with a catalyst.
 45. The process ofclaim 44, wherein catalyzing is achieved using a copper-based catalyst,a Raney nickel-based catalyst, a metal containing organosilica-basedcatalyst, or an iridium complex-based catalyst, or a combinationthereof.
 46. The process of claim 45, wherein catalyzing is achievedusing a co-catalyst, an enhancer, or a promoter, or a combinationthereof.
 47. The process of claim 37, wherein the dehydrogenationreaction and the conversion reaction occur in one reaction vessel; orwherein the dehydrogenation reaction and the conversion reaction occurin more than one reactor vessels, wherein the more than one reactorvessels are functionally connected either continuously ordiscontinuously.
 48. The process of claim 37, wherein the conversionreaction is performed under an inert gas.
 49. The process of claim 48,wherein the inert gas is nitrogen.
 50. The process of claim 37, whereinthe conversion reaction is performed under pressure.
 51. The process ofclaim 50, wherein the conversion reaction is performed under a pressureof 50, 100, 200, 300, 400, 500, 600, 700, 800, 900, 1000, 1100, or 1200psi.
 52. The process of claim 37, wherein the conversion reaction isperformed at a temperature of 50, 60, 70, 80, 90, 100, 110, 120, 130,140, 150, 160, 170, 180, 190, 200, 210, 220, 230, 240, 250, 260, 270,280, 290, or 300° C.
 53. The process of claim 37, wherein the conversionreaction is performed for a time period of 0.1, 0.5, 1, 2, 3, 4, 5, 6,7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22, 23, or 24hours.
 54. The process of claim 37, wherein the biomass-derived moleculeis derived from lignocellulosic biomass.
 55. The process of claim 37,wherein the product comprises at least 50 ppb, 60 ppb, 70 ppb, 80 ppb,90 ppb, 100 ppb, 110 ppb, 120 ppb, 130 ppb, 140 ppb, or 150 ppb of amarker molecule, and wherein the marker molecule is selected from2-butanol, 2-butanone,5-[(1-methylpropoxy)methyl]-2-furancarboxaldehyde,5-hydroxymethyl-2-[(1-methylpropoxy) methyl] furan,2-methyl-5-[(1-methylpropoxy)methyl]furan, or2,5-[bis(1-methylpropoxy)-methyl] furan, or a combination thereof. 56.The process of claim 37, wherein the conversion reaction comprisesconversion of furfural to 1,5-pentanediol.
 57. The process of claim 56,wherein the conversion of furfural to 1,5-pentanediol comprises:contacting furfural with the hydrogen removed during the dehydrogenationreaction in the presence of a first catalyst at a first temperature anda first pressure to yield furfuryl alcohol; and contacting furfurylalcohol with the hydrogen removed during the dehydrogenation reaction inthe presence of a second catalyst at a second temperature and a secondpressure to yield 1,5-pentanediol; wherein the first catalyst and thesecond catalyst, the first temperature and the second temperature, andthe first pressure and the second pressure are the same or different;and wherein the dehydrogenation reaction and the conversion reactionoccur in one reaction vessel, or wherein the dehydrogenation reactionand the conversion reaction occur in more than one reactor vessels,wherein the more than one reactor vessels are functionally connectedeither continuously or discontinuously.
 58. The process of claim 37,wherein the conversion reaction comprises conversion ofhydroxymethylfurfural to 1,6-hexanediol.
 59. The process of claim 58,wherein the conversion of hydroxymethylfurfural to 1,6-hexanediolcomprises: contacting hydroxymethylfurfural with the hydrogen removedduring the dehydrogenation reaction in the presence of a first catalystat a first temperature and a first pressure to yield bi-hydrodroxymethylfuran; contacting bi-hydrodroxymethyl furan with the hydrogen removedduring the dehydrogenation reaction in the presence of a second catalystat a second temperature and a second pressure to yield hexanetriol;contacting hexanetriol with the hydrogen removed during thedehydrogenation reaction in the presence of a third catalyst at a thirdtemperature and a third pressure to yield 1,6-hexanediol; wherein thefirst catalyst, the second catalyst, and the third catalyst; the firsttemperature, the second temperature, and the third temperature; and thefirst pressure, the second pressure, and the third pressure are the sameor different; and wherein the dehydrogenation reaction and theconversion reaction occur in one reaction vessel, or wherein thedehydrogenation reaction and the conversion reaction occur in more thanone reactor vessels, wherein the more than one reactor vessels arefunctionally connected either continuously or discontinuously.
 60. Theprocess of claim 37, wherein the conversion reaction comprisesconversion of 2,4-hydroxybutanoic acid to 1,4-butanediol.
 61. Theprocess of claim 60, wherein the conversion of 2,4-hydroxybutanoic acidto 1,4-butanediol comprises: contacting 2,4-hydroxybutanoic acid withthe hydrogen removed during the dehydrogenation reaction in the presenceof a first catalyst at a first temperature and a first pressure to yield1,2,4-butanetriol; and contacting 1,2,4-butanetriol with the hydrogenremoved during the dehydrogenation reaction in the presence of a secondcatalyst at a second temperature and a second pressure to yield1,4-butanediol; wherein the first catalyst and the second catalyst, thefirst temperature and the second temperature, and the first pressure andthe second pressure are the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected eithercontinuously or discontinuously.
 62. A system configured to perform aprocess to convert a biomass-derived molecule to a conversion product,wherein the process comprises: using a conversion reaction to convertthe biomass-derived molecule to the conversion product; wherein theconversion reaction comprises hydrogenation, hydrogenolysis, orhydrodeoxygenation; and using a dehydrogenation reaction as a source ofhydrogen for the conversion reaction.
 63. The process of claim 62,wherein the dehydrogenation reaction comprises dehydrogenation of2-butanol to 2-butanone.
 64. The process of claim 63, wherein at least40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of2-butanol is dehydrogenated.
 65. The process of claim 64, the percentweight yield of MEK from dehydrogenated 2-butanol is at least 65%, 70%,75%, 80%, 85%, 90%, or 95%.
 66. The process of claim 63, furthercomprising diluting 2-butanol with a solvent, wherein the solvent isinert in the conversion reaction.
 67. The process of claim 66, whereinthe solvent comprises a C₄-C₁₈ hydrocarbon.
 68. The process of claim 67,wherein the C₄-C₁₈ hydrocarbon is selected from hexane, cyclohexane,heptane, octane, decane, or dodecane, or a combination thereof.
 69. Theprocess of claim 62, further comprising catalyzing the dehydrogenationreaction and the conversion reaction with a catalyst.
 70. The process ofclaim 69, wherein catalyzing is achieved using a copper-based catalyst,a Raney nickel-based catalyst, a metal containing organosilica-basedcatalyst, or an iridium complex-based catalyst, or a combinationthereof.
 71. The process of claim 69, wherein catalyzing is achievedusing a co-catalyst, an enhancer, or a promoter, or a combinationthereof.
 72. The process of claim 62, wherein the dehydrogenationreaction and the conversion reaction occur in one reaction vessel; orwherein the dehydrogenation reaction and the conversion reaction occurin more than one reactor vessels, wherein the more than one reactorvessels are functionally connected either continuously ordiscontinuously.
 73. The process of claim 62, wherein the conversionreaction is performed under an inert gas.
 74. The process of claim 73,wherein the inert gas is nitrogen.
 75. The process of claim 62, whereinthe conversion reaction is performed under pressure.
 76. The process ofclaim 75, wherein the conversion reaction is performed under a pressureof 50, 100, 200, 300, 400, 500, 600, 700, 800, 900, 1000, 1100, or 1200psi.
 77. The process of claim 62, wherein the conversion reaction isperformed at a temperature of 50, 60, 70, 80, 90, 100, 110, 120, 130,140, 150, 160, 170, 180, 190, 200, 210, 220, 230, 240, 250, 260, 270,280, 290, or 300° C.
 78. The process of claim 62, wherein the conversionreaction is performed for a time period of 0.1, 0.5, 1, 2, 3, 4, 5, 6,7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 21, 22, 23, or 24hours.
 79. The system of claim 62, wherein the biomass-derived moleculeis derived from lignocellulosic biomass.
 80. The process of claim 62,wherein the conversion reaction comprises conversion of furfural to1,5-pentanediol.
 81. The process of claim 80, wherein the conversion offurfural to 1,5-pentanediol comprises: contacting furfural with thehydrogen removed during the dehydrogenation reaction in the presence ofa first catalyst at a first temperature and a first pressure to yieldfurfuryl alcohol; and contacting furfuryl alcohol with the hydrogenremoved during the dehydrogenation reaction in the presence of a secondcatalyst at a second temperature and a second pressure to yield1,5-pentanediol; wherein the first catalyst and the second catalyst, thefirst temperature and the second temperature, and the first pressure andthe second pressure are the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected eithercontinuously or discontinuously.
 82. The process of claim 62, whereinthe conversion reaction comprises conversion of hydroxymethylfurfural to1,6-hexanediol.
 83. The process of claim 82, wherein the conversion ofhydroxymethylfurfural to 1,6-hexanediol comprises: contactinghydroxymethylfurfural with the hydrogen removed during thedehydrogenation reaction in the presence of a first catalyst at a firsttemperature and a first pressure to yield bi-hydrodroxymethyl furan;contacting bi-hydrodroxymethyl furan with the hydrogen removed duringthe dehydrogenation reaction in the presence of a second catalyst at asecond temperature and a second pressure to yield hexanetriol;contacting hexanetriol with the hydrogen removed during thedehydrogenation reaction in the presence of a third catalyst at a thirdtemperature and a third pressure to yield 1,6-hexanediol; wherein thefirst catalyst, the second catalyst, and the third catalyst; the firsttemperature, the second temperature, and the third temperature; and thefirst pressure, the second pressure, and the third pressure are the sameor different; and wherein the dehydrogenation reaction and theconversion reaction occur in one reaction vessel, or wherein thedehydrogenation reaction and the conversion reaction occur in more thanone reactor vessels, wherein the more than one reactor vessels arefunctionally connected either continuously or discontinuously.
 84. Theprocess of claim 62, wherein the conversion reaction comprisesconversion of 2,4-hydroxybutanoic acid to 1,4-butanediol.
 85. Theprocess of claim 84, wherein the conversion of conversion of2,4-hydroxybutanoic acid to 1,4-butanediol comprises: contacting2,4-hydroxybutanoic acid with the hydrogen removed during thedehydrogenation reaction in the presence of a first catalyst at a firsttemperature and a first pressure to yield 1,2,4-butanetriol; andcontacting 1,2,4-butanetriol with the hydrogen removed during thedehydrogenation reaction in the presence of a second catalyst at asecond temperature and a second pressure to yield 1,4-butanediol;wherein the first catalyst and the second catalyst, the firsttemperature and the second temperature, and the first pressure and thesecond pressure are the same or different; and wherein thedehydrogenation reaction and the conversion reaction occur in onereaction vessel, or wherein the dehydrogenation reaction and theconversion reaction occur in more than one reactor vessels, wherein themore than one reactor vessels are functionally connected eithercontinuously or discontinuously.
 86. The method of claim 12, wherein thecatalyst comprises Pd, Pt, Rh, Ni, Ru, Cu/Si, Cu/zeolite, Cu₂Cr₂O₅,Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al, Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃, Au,lead-aluminum-borate, Raney nickel, Raney nickel/Cu, Raney nickel/Ag,Raney nickel/Au, Raney nickel/Sn, Raney nickel/Pb, Raney nickel/Zn,Raney nickel/Cd, Raney nickel/In, Raney nickel/Ge, MnO, NiO, MgO, Ir,CpIr, CpIr-N-heterocyclic carbene, organosilica, organotitania,organoallumina, organozirconia, Pd—Si—O—Si, Pt—Si—O—Si, Cu—Si—O—Si,Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si, Ir—Si—O—Si, Ag—Si—O—Si,Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or a combination thereof.
 87. Themethod of claim 86, wherein catalyzing the dehydrogenation reaction andthe conversion reaction comprises using a second catalyst, wherein thesecond catalyst comprises Pd, Pt, Rh, Ni, Ru, Cu/Si, Cu/zeolite,Cu₂Cr₂O₅, Ni/Cu/Si, CuO/Al₂O₃, Cu—Fe—Al, Cu—Zn—Al, Cu—Ni, Cu—MgO—Cr₂O₃,Au, lead-aluminum-borate, Raney nickel, Raney nickel/Cu, Raneynickel/Ag, Raney nickel/Au, Raney nickel/Sn, Raney nickel/Pb, Raneynickel/Zn, Raney nickel/Cd, Raney nickel/In, Raney nickel/Ge, MnO, NiO,MgO, Ir, CpIr, CpIr-N-heterocyclic carbene, organosilica, organotitania,organoallumina, organozirconia, Pd—Si—O—Si, Pt—Si—O—Si, Cu—Si—O—Si,Cu—Si—O—Si, Cu₂Cr₂O₅—Si—O—Si, RuSi—O—Si, Ir—Si—O—Si, Ag—Si—O—Si,Fe—Si—O—Si, Co—Si—O—Si, Rh—Si—O—Si, or a combination thereof.
 88. Themethod of any one of claim 86 or 87, wherein catalyzing thedehydrogenation reaction and the conversion reaction further comprisesusing a promoter.
 89. The method of claim 88, wherein the promotercomprises CaO.
 90. The method of any one of claim 88 or 89, wherein thepromoter comprises BaO.
 91. The method of any one of claims 88-90,wherein the promoter comprises ZrO.
 92. The method of any one of claims88-91, wherein the promoter comprises K₂O.
 93. The method of any one ofclaims 88-92, wherein the promoter comprises MgO.
 94. The method of anyone of claims 88-93, wherein the method further comprises diluting2-butanol with a solvent.
 95. The method of claim 94, wherein thesolvent comprises hexane.
 96. The method of any one of claim 94 or 95,wherein the solvent comprises cyclohexane.
 97. The method of any one ofclaims 94-96, wherein the solvent comprises heptane.
 98. The method ofany one of claims 94-97, wherein the solvent comprises octane.
 99. Themethod of any one of claims 94-98, wherein the solvent comprises decane.100. The method of any one of claims 94-99, wherein the solventcomprises dodecane.
 101. The method of any one of claims 94-100, whereinthe solvent comprises isoparaffinic fluids.
 102. A process to convert abiomass-derived molecule to a conversion product, the process comprisingperforming the method of any one of claim 1-36 or 86-101.
 103. A systemconfigured to perform a process to convert a biomass-derived molecule toa conversion product, wherein the process comprises the process of claim102.